CN212548948U - Carbon dioxide capture system - Google Patents
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- CN212548948U CN212548948U CN202021477164.0U CN202021477164U CN212548948U CN 212548948 U CN212548948 U CN 212548948U CN 202021477164 U CN202021477164 U CN 202021477164U CN 212548948 U CN212548948 U CN 212548948U
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Abstract
The utility model belongs to the technical field of gaseous entrapment, concretely relates to carbon dioxide entrapment system. The system comprises a pre-washing tower, a washing liquid recovery device, an absorption tower and a regeneration tower, wherein the washing liquid recovery device is communicated with the pre-washing tower, the washing liquid recovery device comprises a reaction box and a separation box which are communicated, and the reaction box and the separation box are respectively communicated with the pre-washing tower. Be provided with washing liquid recovery unit in this system, can handle the washing liquid, resume the basicity of washing liquid, make its cyclic utilization, the emission of washing liquid has been reduced, the utilization ratio of resource has been improved, can produce calcium-based salt when retrieving the washing liquid, can retrieve as the desulfurizer and recycle, the emission of waste liquid has been reduced, set up washing liquid recovery unit in this system, can realize dual resource recycle, the utilization ratio of resource has been improved, the energy consumption of system has been reduced and the cost of waste liquid treatment has been reduced.
Description
Technical Field
The utility model belongs to the technical field of gaseous entrapment, concretely relates to carbon dioxide entrapment system.
Background
Carbon dioxide is one of the major components of greenhouse gases that contribute to global warming, contributing up to 55% to the greenhouse effect. The carbon dioxide discharged after fossil fuel combustion in a thermal power plant accounts for 30% of the global emission of the same fuel. Thus, the coal fired power plant that emits the most carbon dioxide in the industrial field is the industry with the most potential for carbon dioxide capture. Carbon capture has a variety of technical routes, among which the alcohol amine absorption method is widely used in thermal power generating units.
Because the flue gas discharged by the coal-fired power plant generally comes from a wet desulphurization device or a wet electric precipitation device, the temperature of the flue gas can reach 50-52 ℃ generally, and exceeds the requirement of the proper inlet temperature of an absorption tower of a carbon capture device. Although ultra-clean emissions have been commonly achieved in power plants, the flue gas also contains small amounts of acid gases, such as SO2、SO3HCl and the like, can influence organic amine on CO in the flue gas2Absorption of (2). Therefore, the flue gas must be pretreated first. The pretreatment device is located in CO2Before the absorption tower, a packed tower is generally used, and acid gas in the flue gas is removed by using alkaline washing liquid, and simultaneously, the smoke temperature is reduced. The conventional prewashing liquid is a low-concentration NaOH solution, and the NaOH solution is stronger in alkalinity except for SO2、SO3Reacting with strong acidic gas such as HCl, and optionally CO2The reaction causes additional consumption of alkali and CO in the flue gas2Is lost. After the circulation operation is carried out for a certain time, the pH value of the pre-washing liquid is reduced, and alkali needs to be supplemented in time. The pre-washing liquid can also be enriched with a large amount of sulfate, sulfite and chloride, and the system needs to be discharged in time so as not to influence the pretreatment effect, which can cause a large amount of waste liquid discharge, and the operation of the waste water treatment facility of the power plant is greatly influenced under the condition that the current power plant requires zero discharge of waste water.
Chinese patent document CN110591769A discloses a blast furnace gas catalytic desulfurization device, which comprises a cooling tower, an absorption tower, a regeneration tower, a first liquid circulation pump 7, a filter 8, a cooling tower 1, a solvent absorbent tank 5, a catalyst tank 9, a heat exchanger 10, a second liquid circulation pump 11, a steam boiler 17, and a second spray device; the solvent absorption tank 5 is communicated with the first solvent tank 4, and the catalyst tank 9 and the first solvent tank 4 are both communicated with a liquid inlet of a first liquid circulating pump 7; a first gas-liquid contact device 2, a first spraying device and a first demisting device 6 are sequentially arranged between the gas inlet and the gas outlet at the top of the absorption tower from bottom to top, the liquid outlet of a second liquid circulating pump 11 is connected with the hydrothermal liquid inlet of a heat exchanger 10, and the hydrothermal liquid outlet of the heat exchanger 10 is connected with the second spraying device. But the cooling tower in the device can generate a large amount of waste liquid, and the resource waste is serious.
Disclosure of Invention
Therefore, the to-be-solved technical problem of the utility model lies in overcoming the defects such as the pretreatment system waste water production volume of the carbon dioxide trapping device among the prior art is big, cause the wasting of resources serious to a carbon dioxide trapping system is provided.
Therefore, the utility model provides the following technical scheme.
The utility model provides a carbon dioxide capture system, which comprises,
the pre-washing tower is used for absorbing acid gas in the mixed gas and reducing the temperature of the mixed gas; a washing liquid storage device is arranged at the bottom of the pre-washing tower, and a first washing liquid outlet is formed in the side surface of the washing liquid storage device;
a washing liquid recovery device communicated with the prewashing tower; the washing liquid recovery device comprises a reaction box and a separation box which are communicated, and the reaction box and the separation box are respectively communicated with the prewashing tower;
an absorption tower for absorbing CO in the mixed gas2In communication with the pre-scrubber;
regeneration column for recovery of CO2And is communicated with the absorption tower.
The gas absorbed by the washing liquid in the pre-washing tower is mainly SO2Gas, absorbing a small amount of CO2A gas.
A stirrer is arranged in the reaction box;
a mud scraper is arranged in the separation box, and a slurry outlet is arranged at the bottom of the separation box.
A first packing layer, a first spraying device and a first demisting device are sequentially arranged in the prewashing tower from bottom to top;
the first spraying device is arranged above the washing liquid storage device;
the first washing liquid outlet is communicated with the first spraying device;
the top of the pre-washing tower is provided with a first exhaust port.
And a rich liquid storage device, a second packing layer, a second spraying device, a second demisting device and a second exhaust port are sequentially arranged in the absorption tower from bottom to top.
And a barren solution storage device, a third packing layer, a third spraying device, a third demisting device and a third exhaust port are sequentially arranged in the regeneration tower from bottom to top.
The rich liquid storage device is provided with a rich liquid outlet which is communicated with the third spraying device;
the barren liquor storage device is provided with a barren liquor outlet which is communicated with the second spraying device.
The regeneration tower is also provided with a gas-liquid distribution device, a liquid inlet hole and a liquid outlet hole;
a heater is arranged between the liquid outlet hole and the liquid inlet hole and used for recovering rich liquid;
the gas-liquid distribution device is arranged between the liquid outlet hole and the liquid inlet hole;
the liquid inlet hole is arranged below the third spraying device.
The carbon dioxide capture system also comprises a first heat exchange device, wherein a hot liquid inlet of the first heat exchange device is communicated with the lean liquid outlet, and a hot liquid outlet of the first heat exchange device is communicated with the second spraying device;
and a cold liquid inlet of the first heat exchange device is communicated with the rich liquid outlet, and a cold liquid outlet of the first heat exchange device is communicated with the third spraying device.
The utility model also provides a carbon dioxide capture method, which adopts the carbon dioxide capture system and comprises the following steps,
washing the mixed gas with a washing solution, and then mixing with CO2The gas absorption solvent is contacted to absorb CO2Absorbing the solvent with gas to form a rich solution;
heating the rich liquid after heat exchange to make CO2Gas is separated out, and the rich solution becomes lean solution;
exchanging heat between lean solution and rich solution, cooling, and mixing with CO2Gas contact to absorb CO2A gas.
The carbon dioxide capturing method further includes a step of recovering and reusing the washing liquid.
The utility model discloses technical scheme has following advantage:
1. the utility model provides a carbon dioxide entrapment system, this system include washing tower, washing liquid recovery unit, absorption tower and regeneration tower in advance, washing liquid recovery unit and washing tower intercommunication in advance, and washing liquid recovery unit includes the reaction box and the separator box of intercommunication, and reaction box and separator box communicate with washing tower in advance respectively. Be provided with washing liquid recovery unit in this system, can handle the washing liquid, resume the basicity of washing liquid, make its cyclic utilization, the emission of washing liquid has been reduced, the utilization ratio of resource has been improved, can produce calcium-based salt when retrieving the washing liquid, can retrieve as the desulfurizer and recycle, the emission of waste liquid has been reduced, set up washing liquid recovery unit in this system, can realize dual resource recycle, the utilization ratio of resource has been improved, the energy consumption of system has been reduced and the cost of waste liquid treatment has been reduced.
The washing liquid recovery device has the advantages of small occupied area, small investment and low cost, and the washing liquid can be recycled.
2. The utility model provides a carbon dioxide entrapment system is provided with the agitator in the reaction box, can accelerate the recovery rate of washing liquid in advance, can also prevent the problem that the suspended solid subsides from appearing when washing liquid retrieves in advance simultaneously. A mud scraper is arranged in the separation box, which is helpful for separating liquid and solid in the separation box and preventing calcium-based salts from accumulating and scaling at the bottom.
When the washing liquid in the carbon dioxide capture system is recycled, lime milk can be fed into the reaction box by using a lime milk feeding device of a desulfurization wastewater system which is conventionally matched with an electric field, the washing liquid is recycled, lime milk feeding equipment is not required to be additionally added, the cost for treating the washing liquid is reduced, and the effective utilization of resources is realized. Clear liquid at the upper part of the separation tankThe alkalinity is recovered, and the acid gas is sent to a pre-washing tower to circularly absorb the acid gas in the mixed gas; the concentrated slurry at the bottom of the separation tank is rich in limestone and is pumped to a wet desulphurization absorption tower of a power plant to be used as SO2And (5) recycling the absorbent.
3. The utility model provides a carbon dioxide entrapment method, this method is easy and simple to handle, the energy consumption is few, can also avoid the problem of a large amount of waste liquid emissions.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic view showing the structure of a carbon dioxide capturing system according to example 1 of the present invention;
FIG. 2 is a schematic view of a structure of a prewashing tower according to a second embodiment of example 1 of the present invention;
FIG. 3 is a schematic structural view of a prewashing column according to a third embodiment of example 1 of the present invention;
reference numerals:
1-a prewashing tower; 2-an absorption column; 3-a regeneration tower; 4-a first heat exchange device; 5-a third circulation pump; 6-a fourth circulation pump; 7-a second cooler; 8-a washing liquid recovery device;
1-1-a wash liquor storage device; 1-2-a first packing layer; 1-3-a first spraying device; 1-4-a first defogging device; 1-5-a first exhaust port; 1-6-a first cooler; 1-7-a first circulation pump; 1-8-a first wash liquid outlet; 1-9-a first air inlet; 1-10-pH monitor; 1-11-a first wash liquid inlet; 1-12-a second wash liquid outlet; 1-13-a second wash inlet;
2-1-rich liquid storage device; 2-2-a second packing layer; 2-3-a second spraying device; 2-4-a second demisting device; 2-5-rich liquid outlet; 2-6-a second vent; 2-7-a second air inlet;
3-1-barren liquor storage means; 3-2-gas-liquid distribution device; 3-3-liter air cap; 3-4-a third packing layer; 3-5-a third demisting device; 3-6-a third spraying device; 3-7-liquid outlet holes; 3-8-liquid inlet hole; 3-9-a heater; 3-10-lean solution outlet; 3-11-a third vent;
8-1-reaction box; 8-2-separation tank; 8-3-a second circulation pump; 8-4-fifth circulation pump;
8-1-1-a first liquid inlet; 8-1-2-second liquid inlet; 8-1-3-stirrer; 8-1-4-a first drain outlet; 8-2-1-a second liquid outlet; 8-2-2-mud scraper; 8-2-3-a third liquid inlet; 8-2-4-slurry outlet.
Detailed Description
The following examples are provided for better understanding of the present invention, and are not limited to the best mode, and do not limit the scope and content of the present invention, and any product that is the same or similar to the present invention, which is obtained by combining the features of the present invention with other prior art or the present invention, falls within the scope of the present invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "communicating" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Example 1
The present embodiment provides a carbon dioxide capture system, as shown in fig. 1, comprising,
a pre-washing tower 1 for absorbing acid gas (SO) in the mixed gas2Gas and CO2A gas); a washing liquid storage device 1-1 is arranged in the pre-washing tower 1, andthe washing liquid storage device is respectively provided with a first washing liquid outlet 1-8 and a first air inlet 1-9, the first washing liquid outlet 1-8 is used for discharging washing liquid, and the first air inlet 1-9 sends mixed gas into the pre-washing tower; the prewashing tower is also internally provided with a first spraying device 1-3, a first washing liquid outlet 1-8 is communicated with the first spraying device 1-3 through a first circulating pump 1-7 and a first cooler 1-6, the first cooler 1-6 is used for cooling the washing liquid to keep the temperature of the washing liquid at 38-42 ℃, and the washing liquid is sprayed out of the first spraying device 1-3 after passing through the first circulating pump 1-7 and the first cooler 1-6 to wash the mixed gas and absorb SO in the mixed gas2Gas and CO2A gas; a pH monitor 1-10 is arranged between the first circulating pump 1-7 and the first cooler 1-6 and is used for monitoring the pH value of the washing liquid. In the embodiment, the first air inlet 1-9 is positioned below the first spraying device 1-3, the temperature of the cleaning solution passing through the first cooler is kept at 40 +/-1 ℃, and the mixed gas is in countercurrent contact with the solvent sprayed by the first spraying device 1-3.
A washing liquid recovery device 8 communicated with the prewashing tower 1; the washing liquid recovery device 8 comprises a reaction box 8-1 and a separation box 8-2 which are communicated, the reaction box 8-1 is communicated with the prewashing tower 1 through a first washing liquid outlet 1-8 and a first circulating pump 1-7, the first circulating pump 1-7 pumps part of washing liquid into the reaction box 8-1 for recovery, a stirrer 8-1-3 is further arranged in the reaction box 8-1, and the stirrer 8-1-3 is used for stirring the washing liquid in the reaction box 8-1 to promote the washing liquid to fully react with lime milk, so that the recovery rate of the washing liquid is improved, and meanwhile, the bottom of the washing tank is prevented from depositing; the reaction box 8-1 is also provided with a first liquid inlet 8-1-1 for introducing a solvent for recovering the washing liquid into the reaction box 8-1; the washing liquid in the prewashing tower flows into the reaction box 8-1 from the second liquid inlet 8-1-2 of the reaction box through the first circulating pump 1-7 to react, the washing liquid after the reaction flows out from the first liquid outlet 8-1-4 and flows into the separation box 8-2 through the third liquid inlet 8-2-3, the mud scraper 8-2-2 is arranged in the separation box 8-2, the mud scraper 8-2-2 is driven by a motor to rotate slowly, so that the bottom of the separation box can be prevented from accumulating and scaling, solid-liquid separation is facilitated, the recovered washing liquid and slurry are obtained after separation, the recovered washing liquid is discharged from the second liquid outlet 8-2-1 and is discharged from the first washing towerThe washing liquid flowing out of the liquid outlets 1-8 is converged, the slurry is pumped out by the second circulating pump 8-3, and the slurry can be used for treating SO2The gas and the second circulating pump are mainly used for recycling the slurry. When a pH monitor 1-10 monitors that the pH of the washing liquid is between 7 and 9, discharging part of the washing liquid into a washing liquid recovery device for recovery, and enabling the recovered washing liquid to flow into a pre-washing tower again, specifically, the washing liquid flows out from a first circulating pump 1-7 and is divided into two branches, the first branch flows through a first cooler 1-6 and then is sprayed out from a first spraying device 1-3, the second branch flows into a reaction box 8-1 for reaction, the reacted washing liquid enters a separation box 8-2 for separation to obtain the recovered washing liquid and slurry, the recovered washing liquid is discharged from a second liquid outlet 8-2-1, is converged with the washing liquid flowing out from a first washing liquid outlet 1-8 and then enters the first circulating pump 1-7 again, and the valve opening of the first branch and the second branch on the first circulating pump outlet is adjusted, and adjusting the flow rates of the first branch flow and the second branch flow so as to control the recovery amount of the washing liquid. In this embodiment, when the pH is less than 8, the washing solution is recovered, the washing solution can be, but is not limited to, an alkaline solvent, the washing solution in this embodiment is a NaOH solution, and the NaOH solution absorbs the acidic gas (SO) in the mixed gas2And CO2Gas) to form three solutions of sodium sulfate, sodium sulfite and sodium carbonate; the solvent for recycling the washing liquid is slaked lime solution, the slaked lime can be added by using the existing lime milk adding device, the slaked lime enters the reaction box 8-1 from the first liquid inlet 8-1-1, the slaked lime respectively reacts with sodium sulfate, sodium sulfite and sodium carbonate to obtain NaOH solution and slurry (the main components are calcium sulfite, calcium sulfate and calcium carbonate), the NaOH solution is recycled, when the concentration of the slurry reaches 5-10 wt%, the slurry is discharged from the slurry outlet 8-2-4 and can be used for recycling SO in a desulfurization absorption system2The second liquid outlet 8-2-1 is communicated with the first washing liquid outlet 1-8; the level of the liquid level in the reaction box is higher than that in the separation box; the ratio of the flow rate of the first substream to the flow rate of the second substream is 9: 1; the liquid level of the washing liquid in the reaction box 8-1 is higher than that of the washing liquid in the separation box 8-2, and the washing liquid in the separation box 8-2The liquid level is higher than the liquid level in the washing liquid storage device 1-1, and the washing liquid flows into the separation box from the reaction box and then flows into the washing liquid storage device under the action of gravity.
An absorption tower 2 for absorbing CO in the mixed gas2And is communicated with the prewashing tower.
A regeneration tower 3 for regenerating CO2Absorption of solvent and recovery of CO2And is communicated with the absorption tower.
As another alternative, as shown in FIG. 2, a second washing liquid inlet 1-13 is further provided on the washing liquid storage device 1-1 of the pre-washing tower 1, the separation tank 8-2 is communicated with the washing liquid storage device 1-1 through a second liquid outlet 8-2-1, the separation tank 8-2 separates the washing liquid after washing the gas to obtain the recovered washing liquid and slurry, and the recovered washing liquid is recovered to the pre-washing tower through a second washing liquid inlet 1-13 for recycling.
As another alternative, as shown in FIG. 3, the washing liquid storage means 1-1 of the prewashing tower 1 is further provided with a second washing liquid outlet 1-12 and a first washing liquid inlet 1-11; the reaction box 8-1 is communicated with the second washing liquid outlet 1-12 through a fifth circulating pump 8-4, the separation box 8-2 is communicated with the first washing liquid inlet 1-11, when the pH of the washing liquid is between 7 and 9, under the action of the fifth circulating pump 8-4, part of the washing liquid is controlled to be discharged from the second washing liquid outlet, part of the washing liquid enters the washing liquid recovery device to be recovered, the part of the washing liquid firstly enters the reaction box 8-1 to react and then enters the separation box 8-2 to be separated, the separated washing liquid flows into the washing liquid storage device 1-1 through the first washing liquid inlet 1-11 again to be recycled, and the washing effect of the washing liquid is improved.
As a preferable embodiment, a first packing layer 1-2 and a first demisting device 1-4 are also arranged in the prewashing tower 1, the first packing layer 1-2 is arranged above the washing liquid storage device 1-1, the first packing layer 1-2 is arranged below the first spraying device 1-3, and the first demisting device 1-4 is arranged above the first spraying device 1-3; the first filler layer 1-2 can be one layer or a plurality of layers; the material of the first filler layer 1-2 is random packing; in the embodiment, the first packing layer is a layer made of PP plastic, and the first demisting device is a stainless steel wire mesh demister; the first inlet openings 1-9 are located below the first packing layer.
In a preferred embodiment, the top of the prewash tower 1 is provided with a first exhaust port 1-5, the absorption tower 2 is provided with a second intake port 2-7, and the prewash tower 1 and the absorption tower 2 are communicated through the first exhaust port 1-5 and the second intake port 2-7.
As a preferable embodiment, a rich liquid storage device 2-1, a second packing layer 2-2, a second spraying device 2-3 and a second demisting device 2-4 are sequentially arranged in the absorption tower from bottom to top, a second gas outlet 2-6 is further arranged at the top of the absorption tower, and the second packing layer 2-2 is made of random or structured packing and can be a layer or a plurality of layers. In the embodiment, the second packing layer 2-2 is two layers and is made of a structured packing layer, the second demister 2-4 is a stainless steel wire gauze demister, and the second air inlet is positioned below the second packing layer; for absorbing CO2The gas solvent is alcohol amine solution, specifically organic amine mixed solution of monoethanolamine MEA, hindered amine AMP and piperazine PZ with molar ratio of 1:1:1, and absorbs CO2Forming a rich solution from the alcohol amine solution after the gas is gasified, and storing the rich solution in a rich solution storage device; the alcohol amine solution is sprayed out from the second spraying device to absorb CO in a countercurrent manner2A gas.
As a preferred embodiment, the carbon dioxide capturing system further comprises a first heat exchange device 4, and the absorption tower 2 and the regeneration tower 3 are communicated through the first heat exchange device 4; the absorption tower 2 is also provided with a rich liquid outlet 2-5, the regeneration tower 3 is provided with a lean liquid outlet 3-10 and a third spraying device 3-6, a hydrothermal inlet of the first heat exchange device 4 is communicated with the lean liquid outlet 3-10 through a fourth circulating pump 6, a hydrothermal outlet is communicated with the second spraying device 2-3 through a second cooler 7, a cold liquid inlet of the first heat exchange device 4 is communicated with the rich liquid outlet 2-5 through a third circulating pump 5, and a cold liquid outlet is communicated with the third spraying device 3-6; the rich liquid is sprayed out from the third spraying devices 3-6 after heat exchange by the first heat exchange device 4. The temperature in the regeneration tower is high, which is beneficial to CO2The gas is separated out from the rich liquid, the temperature in the absorption tower is low, and the CO is favorably separated out2Absorption of gas intoBefore the raw tower, the temperature of the rich solution can be increased and the temperature of the lean solution can be reduced after the heat exchange between the rich solution and the lean solution, which is beneficial to absorbing CO in the tower2CO absorption and regeneration tower for gas2The separation of the gas and the heat exchange between the rich solution and the lean solution can also reduce the energy loss caused by heating the rich solution and cooling the lean solution.
As a preferable embodiment, a barren solution storage device 3-1, a gas-liquid distribution device 3-2, a third packing layer 3-4 and a fourth demisting device 3-5 are arranged in the regeneration tower from bottom to top, and a third spraying device 3-6 is arranged between the third packing layer 3-4 and the fourth demisting device 3-5; the gas-liquid distribution device 3-2 is also provided with a gas lifting cap 3-3, the gas lifting cap 3-3 is used for preventing the liquid sprayed by the third spraying device 3-6 from flowing into the barren solution storage device 3-1 and ensuring CO separated out from the tower bottom2The gas may flow from bottom to top. The regeneration tower is also provided with a liquid inlet hole 3-8 and a liquid outlet hole 3-7, the liquid inlet hole 3-8 and the liquid outlet hole 3-7 are respectively arranged at two sides of the gas-liquid distribution device 3-2, the liquid inlet hole 3-8 is arranged below the gas-liquid distribution device 3-2, a heater 3-9 is also arranged between the liquid inlet hole 3-8 and the liquid outlet hole 3-7, rich liquid is sprayed out from the third spraying device 3-6, stored on the gas-liquid distribution device after passing through a third packing layer, and enters the heater 3-9 through the liquid outlet hole 3-7 to be heated, so that CO in the rich liquid is sprayed out from the third spraying device 3-6 and then enters the2Separating out gas, changing rich solution into lean solution, feeding into lean solution storage device 3-1, and separating out CO2The gas is exhausted from a third exhaust port 3-11 after passing through the air lifting cap, the third packing layer and the third demisting device; the material of the third packing layers 3-4 is structured packing, which can be one layer or a plurality of layers. In this embodiment, the third packing layers 3 to 4 are made of stainless steel structured packing and have two layers, and the third demister is a stainless steel wire mesh demister.
Example 2
This example provides a method for capturing carbon dioxide using the carbon dioxide capturing system (fig. 1) provided in example 1, comprising the steps of,
the washing liquid flows out from the first washing liquid outlet and is sprayed out from the first spraying device, the mixed gas is introduced into the pre-washing tower 1 through the first gas inlet, and the mixed gas and the washing liquid are in countercurrent contact to washWashing liquid for absorbing SO in mixed gas2Gas and part of CO2Monitoring the pH value of the washing liquid during the washing process, when the pH value of the washing liquid is lower than 8, dividing the first circulating pump into a first branch flow and a second branch flow, wherein the flow ratio of the first branch flow to the second branch flow is 9:1, spraying the washing mixed gas from the first spraying device by the first branch flow, enabling the second branch flow to flow into a reaction box 8-1 to react with slaked lime, enabling the reacted washing liquid to flow into a separation box to be separated to obtain the recycled washing liquid and slurry, enabling the washing liquid to enter the first circulating pump after being merged with the washing liquid flowing out of a washing liquid outlet until the pH value of the washing liquid reaches 11, stopping introducing the washing liquid into a washing liquid recycling device, and discharging the slurry for recycling;
the washed mixed gas is conveyed into the absorption tower, the mixed gas flows from bottom to top, and the ethanolamine solution in the absorption tower is sprayed out from the second spraying device and is mixed with CO2Gas countercurrent contact for absorbing CO2Forming a rich solution by the ethanolamine solution after the gas is generated, storing the rich solution in a rich solution storage device, and exhausting the residual gas from a second exhaust port;
the rich liquid enters the regeneration tower after heat exchange, is sprayed out from the third spraying device, and after heating, CO is enabled to be generated2Gas is separated out from the rich solution, the rich solution forms a barren solution, the barren solution is stored in a barren solution storage device, flows out of the regeneration tower, enters the absorption tower after heat exchange, is sprayed out from the second spraying device, and reversely absorbs CO2A gas; recovered CO2And the gas is discharged from the third exhaust port and collected.
Example 3
This example provides a method for capturing carbon dioxide using the carbon dioxide capturing system (shown in fig. 3) provided in example 1, comprising the steps of,
the cleaning solution flows out through a first cleaning solution outlet and is sprayed out from a first spraying device, the mixed gas is introduced into the prewashing tower 1 through a first gas inlet, the mixed gas is in countercurrent contact with the cleaning solution, and the cleaning solution absorbs SO in the mixed gas2Gas and part of CO2Gas, during which the pH value of the washing liquid is monitored, and when the pH value of the washing liquid is lower than 8, a fifth circulation pump pumps part of the washing liquid into the reverse circulation pumpReacting the reaction product in the reaction tank 8-1 with slaked lime, then enabling the washing liquid after the reaction to flow into a separation tank for separation to obtain recycled washing liquid and slurry, enabling the recycled washing liquid to flow into a washing liquid storage device 1-1 through a first washing liquid inlet 1-11, recycling the washing liquid until the pH value reaches 10, stopping introducing the washing liquid into a washing liquid recycling device, and recycling the slurry after the slurry is discharged;
the washed mixed gas is conveyed into the absorption tower, the mixed gas flows from bottom to top, and the ethanolamine solution in the absorption tower is sprayed out from the second spraying device and is mixed with CO2Gas countercurrent contact for absorbing CO2Forming a rich solution by the ethanolamine solution after the gas is generated, storing the rich solution in a rich solution storage device, discharging the residual gas from a second gas outlet, and collecting the residual gas;
the rich liquid enters the regeneration tower after heat exchange, is sprayed out from the third spraying device, and after heating, CO is enabled to be generated2Gas is separated out from the rich solution, the rich solution forms a barren solution which is stored in a barren solution storage device, the barren solution flows out of the regeneration tower, enters the absorption tower after heat exchange, is sprayed out from the second spraying device, and absorbs CO in a countercurrent mode2A gas.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the spirit or scope of the invention.
Claims (8)
1. A carbon dioxide capture system, comprising,
the pre-washing tower is used for absorbing acid gas in the mixed gas and reducing the temperature of the mixed gas; a washing liquid storage device is arranged at the bottom of the pre-washing tower, and a first washing liquid outlet is formed in the side surface of the washing liquid storage device;
a washing liquid recovery device communicated with the prewashing tower; the washing liquid recovery device comprises a reaction box and a separation box which are communicated, and the reaction box and the separation box are respectively communicated with the prewashing tower;
an absorption tower for absorbing CO in the mixed gas2In communication with the pre-scrubber;
regeneration column for recovery of CO2And is communicated with the absorption tower.
2. The carbon dioxide capture system of claim 1, wherein an agitator is disposed within the reaction tank;
a mud scraper is arranged in the separation box, and a slurry outlet is arranged at the bottom of the separation box.
3. The carbon dioxide capture system of claim 1 or 2, wherein a first packing layer, a first spraying device and a first demisting device are arranged in the prewashing tower from bottom to top in sequence;
the first spraying device is arranged above the washing liquid storage device;
the first washing liquid outlet is communicated with the first spraying device;
the top of the pre-washing tower is provided with a first exhaust port.
4. The carbon dioxide capture system according to claim 1 or 2, wherein a rich liquid storage device, a second packing layer, a second spraying device, a second demisting device and a second exhaust port are arranged in the absorption tower from bottom to top in sequence.
5. The carbon dioxide capture system of claim 4, wherein the lean solution storage device, the third packing layer, the third spraying device, the third demisting device and the third exhaust port are arranged in the regeneration tower from bottom to top in sequence.
6. The carbon dioxide capture system of claim 5, wherein the rich liquid storage device is provided with a rich liquid outlet, the rich liquid outlet being in communication with the third spraying device;
the barren liquor storage device is provided with a barren liquor outlet which is communicated with the second spraying device.
7. The carbon dioxide capture system of claim 5, wherein the regeneration tower is further provided with a gas-liquid distribution device, a liquid inlet aperture and a liquid outlet aperture;
a heater is arranged between the liquid outlet hole and the liquid inlet hole and used for recovering rich liquid;
the gas-liquid distribution device is arranged between the liquid outlet hole and the liquid inlet hole;
the liquid inlet hole is arranged below the third spraying device.
8. The carbon dioxide capture system of claim 6, further comprising a first heat exchange device having a hot liquid inlet in communication with the lean liquid outlet and a hot liquid outlet in communication with the second spray device;
and a cold liquid inlet of the first heat exchange device is communicated with the rich liquid outlet, and a cold liquid outlet of the first heat exchange device is communicated with the third spraying device.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113109126A (en) * | 2021-03-09 | 2021-07-13 | 中国环境科学研究院 | Phosphate oxygen isotope enrichment equipment, method and device |
| CN114669177A (en) * | 2022-03-09 | 2022-06-28 | 中国矿业大学 | Low-energy-consumption CO2Trapping and compression refining process |
-
2020
- 2020-07-23 CN CN202021477164.0U patent/CN212548948U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113109126A (en) * | 2021-03-09 | 2021-07-13 | 中国环境科学研究院 | Phosphate oxygen isotope enrichment equipment, method and device |
| CN114669177A (en) * | 2022-03-09 | 2022-06-28 | 中国矿业大学 | Low-energy-consumption CO2Trapping and compression refining process |
| CN114669177B (en) * | 2022-03-09 | 2024-01-26 | 中国矿业大学 | Low-energy-consumption CO 2 Trapping and compression refining process |
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