CN219907006U - Carbon trapping device - Google Patents
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- CN219907006U CN219907006U CN202320080590.8U CN202320080590U CN219907006U CN 219907006 U CN219907006 U CN 219907006U CN 202320080590 U CN202320080590 U CN 202320080590U CN 219907006 U CN219907006 U CN 219907006U
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Abstract
The utility model relates to a carbon trapping device, which comprises a compression assembly, a drying assembly, a rectifying assembly and an adjusting valve assembly, wherein the compression assembly, the drying assembly and the rectifying assembly are sequentially arranged along the flowing direction of raw gas: the drying assembly comprises three dryers which are sequentially connected, wherein the dryers are respectively connected with a drying pipeline, a back blowing pipeline and a regeneration pipeline, the drying pipelines, the back blowing pipelines and the regeneration pipelines in the dryers are respectively and independently started, and the starting states of the drying pipelines, the back blowing pipelines and the regeneration pipelines in the dryers are different and are alternatively started. The utility model compresses, dries and rectifies the raw material gas, liquefies the carbon dioxide in the raw material gas, and realizes continuous, efficient and high-purity carbon dioxide capture.
Description
Technical Field
The utility model relates to the technical field of carbon dioxide recovery, in particular to a carbon capture device.
Background
Carbon capture is to purify carbon dioxide discharged in the production process, then put into a new production process, and recycle the carbon dioxide instead of simply sealing the carbon dioxide in tail gas discharged and combusted by a chimney of a power plant or a steel plant.
In the conventional art, the carbon capturing method includes a solid absorption method, a solvent adsorption method, a membrane method, and a low temperature rectification method. The solid adsorption method is divided into pressure swing adsorption and temperature swing adsorption, and high-performance adsorbent is needed, so that the product purity is low; solvent absorption methods include chemical absorption, physical absorption, and physicochemical absorption, but the energy consumption is high; the principle of the membrane separation method is to separate carbon dioxide by utilizing the properties of membrane materials, but the membrane component has high requirements, short service life and low product purity.
Therefore, how to provide a capturing device for capturing carbon dioxide with high efficiency is an urgent problem to be solved at present.
Disclosure of Invention
Based on this, it is necessary to provide a carbon capture device that achieves continuous, efficient and high purity capture of carbon dioxide.
The specific scheme for solving the technical problems is as follows:
the utility model provides a carbon capture device, which comprises a compression assembly, a drying assembly, a rectifying assembly and an adjusting valve assembly, wherein the compression assembly, the drying assembly and the rectifying assembly are sequentially arranged along the flowing direction of raw gas:
a compression assembly for pressurizing the feed gas;
the drying assembly comprises three dryers which are sequentially connected, and the dryers are connected with a drying pipeline, a back blowing pipeline and a regeneration pipeline;
the compression assembly is connected with the drying assembly through a connecting main pipe, the output end of the connecting main pipe is connected with a first branch pipeline and a second branch pipeline in parallel, the first branch pipeline is respectively connected with the input end of the back blowing pipeline of each dryer, and the second branch pipeline is respectively connected with the input end of the drying pipeline of each dryer;
the drying pipeline, the back flushing pipeline and the regeneration pipeline in the dryer are respectively and independently started, and the starting states of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer are different and are alternatively started;
the drying assembly further comprises a regeneration gas heater and cooling dehydrators, wherein the output ends of the back blowing pipelines in the dryers are connected with the regeneration gas heater, the regeneration gas heater is used for heating the back-blown gas, the output ends of the regeneration gas heater are respectively connected with the input ends of the regeneration pipelines in the dryers, the output ends of the regeneration pipelines in the dryers are connected with the cooling dehydrators, the cooling dehydrators are used for cooling liquid in liquefied removal gas, and the gas output ends of the cooling dehydrators are connected with the second branch pipeline;
the regulating valve assembly comprises a control valve arranged on a pipeline of the drying assembly and is used for switching the closing and starting of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer;
and the rectification component is used for rectifying and purifying the dry gas output by the drying component.
In some embodiments, in the drying assembly, the drying pipeline comprises a drying air inlet pipe connected to the top of the dryer and a drying air outlet pipe connected to the bottom of the dryer, the back-blowing pipeline comprises a back-blowing air inlet pipe connected to the bottom of the dryer and a back-blowing air outlet pipe connected to the top of the dryer, and the regeneration pipeline comprises a regeneration air inlet pipe connected to the bottom of the dryer and a regeneration air outlet pipe connected to the top of the dryer.
The first branch pipelines are respectively and independently connected with the back blowing air inlet pipes of the dryers, and the second branch pipelines are respectively and independently connected with the drying air inlet pipes of the dryers.
The back-blowing air outlet pipes of the dryers are all connected with the regenerated gas heater, the air outlet ends of the regenerated gas heater are respectively and independently connected with the regenerated air inlet pipes of the dryers, the regenerated air outlet pipes of the dryers are all connected with the cooling dehydrator, and the gas phase output ends of the cooling dehydrator are connected with the second branch pipeline.
In some embodiments, the compression assembly comprises at least two compressors, and the output ends of the compressors are respectively provided with a cooler and a gas-liquid separator which are connected in sequence.
In some embodiments, the compression assembly comprises a first stage compressor and a second stage compressor along the flow direction of the feed gas, and the output end of the first stage compressor and the output end of the second stage compressor are sequentially provided with a cooler and a gas-liquid separator.
The gas-liquid separator at the output end of the first stage compressor is connected to the input end of the first stage compressor through a liquid circulation pipeline, and the liquid circulation pipeline is connected with the liquid phase output end of the gas-liquid separator.
In some embodiments, a pressure reducer is provided on the liquid circulation line.
In some embodiments, the cooling water trap comprises a regeneration gas cooler and a regeneration gas knockout connected in sequence.
In some embodiments, an cascade refrigeration unit is disposed between the rectification assembly and the drying assembly, the cascade refrigeration unit including a cryocooler and a cryocooler, the cryocooler configured to cool and liquefy the dry gas entering the rectification assembly.
In some embodiments, the rectification component comprises a rectification column, the high temperature refrigerator is arranged at the bottom of the rectification column, and the high temperature refrigerator is used for cooling liquid phase products output by the rectification column.
In some embodiments, the gas input end of the cascade refrigeration unit is provided with a recuperation heat exchanger, and the dry gas output by the drying assembly enters a heat source pipeline of the recuperation heat exchanger as a heat source.
In some embodiments, the recuperation heat exchanger comprises at least two stages of heat exchange chambers, and the gas-phase product of the rectifying tower sequentially enters each heat exchange chamber to exchange heat and raise temperature.
In some embodiments, the gas line between adjacent heat exchange chambers is provided with a pressure reducer for reducing the pressure of the warmed gas phase product.
The utility model has the following beneficial effects:
the utility model adopts the compression component, the drying component, the rectifying component and the regulating valve component to sequentially compress, dry and rectify the raw material gas, liquefy the carbon dioxide in the raw material gas, and further obtain high-purity carbon dioxide in the rectifying component.
Drawings
FIG. 1 is a schematic view of a carbon capture apparatus according to an embodiment of the present utility model;
FIG. 2 is a schematic view showing a structure of a drying unit in the carbon capture apparatus according to an embodiment of the present utility model;
FIG. 3 is a schematic view of a compression assembly in a carbon capture apparatus according to one embodiment of the present utility model;
fig. 4 is a schematic structural diagram of a rectifying component and a recuperative heat exchanger in a carbon capture device according to an embodiment of the present utility model.
Wherein, 100-compressing the assembly; 101-a first stage compressor; 102-a second stage compressor; 103-first stage cooler; 104-a first-stage gas-liquid separator; 105-a second stage cooler; 106-a second-stage gas-liquid separator; 107-a first pressure reducer; 200-drying the assembly; 201-a first dryer; 202-a second dryer; 203-a third dryer; 204-a first branch line; 205-a second branch line; 206-drying the air inlet pipe; 207-drying the air outlet pipe; 208-back blowing an air inlet pipe; 209-back blowing an air outlet pipe; 210-regenerating an air inlet pipe; 211-a regenerated air outlet pipe; 212-a regeneration gas heater; 213-regeneration gas cooler; 214-a regeneration gas knockout; 300-rectifying component; 301-rectifying tower; 302-cryorefrigerator; 303-high temperature refrigerator; 400-reheating heat exchanger; 401-a heat exchange chamber; 402-a second pressure reducer.
Detailed Description
In order that the above objects, features and advantages of the utility model will be readily understood, a more particular description of the utility model will be rendered by reference to the appended drawings. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present utility model. The present utility model may be embodied in many other forms than described herein and similarly modified by those skilled in the art without departing from the spirit of the utility model, whereby the utility model is not limited to the specific embodiments disclosed below.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present utility model, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
It will be understood that when an element is referred to as being "fixed" or "disposed" on another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like are used herein for illustrative purposes only and are not meant to be the only embodiment.
In one embodiment, the present utility model provides a carbon capture apparatus, as shown in fig. 1, including a compression assembly 100, a drying assembly 200, a rectification assembly 300, and a regulating valve assembly (not shown in the drawing), where the compression assembly 100, the drying assembly 200, and the rectification assembly 300 are sequentially disposed along a flow direction of a raw material gas:
a compression assembly 100, the compression assembly 100 for pressurizing a feed gas;
the drying assembly 200 comprises three dryers which are sequentially connected, wherein the dryers are connected with a drying pipeline, a back blowing pipeline and a regeneration pipeline;
the compression assembly 100 is connected with the drying assembly 200 through a connecting main pipe, the output end of the connecting main pipe is connected with a first branch pipeline 204 and a second branch pipeline 205 in parallel, the first branch pipeline 204 is respectively connected with the input ends of the back-blowing pipelines of the dryers, and the second branch pipeline 205 is respectively connected with the input ends of the drying pipelines of the dryers;
the drying pipeline, the back flushing pipeline and the regeneration pipeline in the dryer are respectively and independently started, and the starting states of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer are different and are alternatively started;
the drying assembly 200 further includes a regeneration gas heater 212 and a cooling dehydrator, the output end of the blowback pipeline in each dryer is connected to the regeneration gas heater 212, the regeneration gas heater 212 is used for heating the gas after blowback, the output end of the regeneration gas heater 212 is respectively connected to the input end of the regeneration pipeline in each dryer, the output end of the regeneration pipeline in each dryer is connected to the cooling dehydrator, the cooling dehydrator is used for cooling the liquid in the liquefied removal gas, and the gas output end of the cooling dehydrator is connected to the second branch pipeline 205;
the regulating valve assembly comprises a control valve arranged on a pipeline of the drying assembly and is used for switching the closing and starting of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer;
and the rectification assembly 300 is used for rectifying and purifying the dry gas output by the drying assembly 200.
The utility model adopts the modes of compression, drying and rectification to trap carbon in the raw material gas, three dryers are adopted in the drying process, part of the raw material gas enters one of the dryers for adsorption drying, and the other part of the raw material gas is used as purge regeneration gas to enter the other two dryers in sequence, and back-blowing pre-drying and back-blowing regeneration are respectively carried out in the two dryers, wherein the gas after back-blowing pre-drying is heated to be used as regeneration gas for back-blowing regeneration, and the regenerated gas is cooled and separated into liquid and then is combined with the raw material gas again for drying, namely the three dryers respectively carry out adsorption drying, back-blowing pre-drying and back-blowing regeneration, so that the continuous drying process is realized, the moisture in the raw material gas is effectively removed, and the efficient and high-purity carbon dioxide trapping is realized.
It should be noted that the raw gas in the utility model can be oil field associated gas, flue gas, chemical tail gas and the like which are rich in CO 2 Is a gas of (a) a gas of (b).
It should be noted that, the drying pipeline, the blowback pipeline and the regeneration pipeline in the dryer of the present utility model are started and closed, which represents the pipeline name that the dryer is connected, and further, the dryer is in different working states due to different connecting pipelines, for example, the dryer of which the drying pipeline is started represents that the dryer is in an adsorption drying state, the gas entering the dryer through the input end of the drying pipeline is dried, and the dried gas is discharged from the dryer and is output through the output end of the drying pipeline.
It should be noted that, in the present utility model, the adjusting valve assembly includes adjusting valves disposed on each pipeline, and the operating states of different dryers are switched by opening and closing the valves, so as to implement the continuous drying process of the drying assembly 200.
In some embodiments, as shown in fig. 2, in the drying assembly 200, the drying pipeline includes a drying air inlet pipe 206 connected to the top of the dryer and a drying air outlet pipe 207 connected to the bottom of the dryer, the blowback pipeline includes a blowback air inlet pipe 208 connected to the bottom of the dryer and a blowback air outlet pipe 209 connected to the top of the dryer, and the regeneration pipeline includes a regeneration air inlet pipe 210 connected to the bottom of the dryer and a regeneration air outlet pipe 211 connected to the top of the dryer.
The first branch pipes 204 are respectively and independently connected with the back-blowing air inlet pipes 208 of the dryers, and the second branch pipes 205 are respectively and independently connected with the drying air inlet pipes 206 of the dryers.
The blowback outlet pipes 209 of the dryers are all connected into the regenerated gas heater 212, the outlet ends of the regenerated gas heater 212 are respectively and independently connected into the regenerated air inlet pipes 210 of the dryers, the regenerated air outlet pipes 211 of the dryers are all connected into the cooling dehydrator, and the gas phase output ends of the cooling dehydrators are connected into the second branch pipeline 205.
Illustratively, an operation state of the three dryers is provided, the drying assembly 200 includes three dryers, namely, a first dryer 201, a second dryer 202 and a third dryer 203, wherein a drying air inlet pipe 206 and a drying air outlet pipe 207 of the first dryer 201 are opened, and the first dryer 201 is in an adsorption drying state; the regenerated gas inlet pipe 210 and the regenerated gas outlet pipe 211 of the second dryer 202 are both opened, and the second dryer 202 is in a regenerated state; the blowback air inlet pipe 208 and the blowback air outlet pipe 209 of the third dryer 203 are both opened, and the third dryer 203 is in a blowback predrying state. Further, the flow direction of the raw material gas is as follows: the raw material gas is compressed and then is divided into back blowing gas and dry gas through a first branch pipeline 204 and a second branch pipeline 205, wherein the back blowing gas enters the third dryer 203 through a back blowing gas inlet pipe 208 in the first branch pipeline 204 and the third dryer 203, the back blowing gas is pre-dried, the pre-dried back blowing gas enters a regeneration gas heater 212 through a back blowing gas outlet pipe 209, the back blowing gas is warmed to form regeneration gas, the regeneration gas enters the second dryer 202 through a regeneration gas inlet pipe 210 of the second dryer 202 for back blowing regeneration, and after cooling and liquid separation, the regenerated gas is collected into the second branch pipeline 205 and the dry gas to be mixed into the first dryer 201 for adsorption drying.
In the utility model, each dryer is sequentially switched from an adsorption drying state, a back-blowing pre-drying state and a regeneration state, namely, the dryer after adsorption drying is used for a period of time and then is used as a back-blowing pre-drying dryer, and the back-blowing pre-drying dryer is used for a period of time and then is subjected to regeneration treatment. The utility model does not make specific requirements and special restrictions on the use time, and a person skilled in the art can reasonably select the state switching time according to the actual processing state.
The dryer may be a dehydration tower, for example.
In some embodiments, the compression assembly 100 includes at least two compressors, and the output ends of the compressors are respectively provided with a cooler and a gas-liquid separator which are connected in sequence. The utility model adopts a multistage compression mode, and separates and discharges partial liquid phase products after each compression, so that the raw material gas can be compressed to 5.0 MPa-6.0 MPa, higher compression pressure is realized, and the capture purity of carbon dioxide is ensured.
In some embodiments, as shown in fig. 3, the compression assembly 100 includes a first stage compressor 101 and a second stage compressor 102 along the flow direction of the raw gas, where the output end of the first stage compressor 101 and the output end of the second stage compressor 102 are sequentially provided with a cooler and a gas-liquid separator.
The gas-liquid separator at the output end of the first stage compressor 101 is connected to the input end of the first stage compressor 101 through a liquid circulation pipeline, and the liquid circulation pipeline is connected with the liquid phase output end of the gas-liquid separator. The liquid circulation line is provided with a pressure reducer, such as the first pressure reducer 107 in fig. 3, which may be a pressure reducing valve. For example, the output end of the first-stage compressor 101 is provided with a first-stage cooler 103 and a first-stage gas-liquid separator 104 in order, and the output end of the second-stage compressor 102 is provided with a second-stage cooler 105 and a second-stage gas-liquid separator 106 in order. Further, the first stage compressor 101 may be a water injection screw compressor, and the second stage compressor 102 may be a reciprocating compressor, with both stages of compression being single stage compression.
In the utility model, a liquid circulation pipeline is adopted in the first-stage compressor 101, and the liquid product after the first-stage compression is subjected to reduced pressure reflux, so that the recovery rate of carbon dioxide is improved.
In some embodiments, the cooling water trap includes a regeneration gas cooler 213 and a regeneration gas knockout 214 connected in sequence.
In some embodiments, as shown in fig. 4, an cascade refrigeration unit is disposed between the rectification unit 300 and the drying unit 200, and the cascade refrigeration unit includes a cryocooler 302 and a high temperature refrigerator 303, and the cryocooler 302 is used for cooling and liquefying the dry gas entering the rectification unit 300.
In some embodiments, the rectification assembly 300 includes a rectification column 301, the high temperature refrigerator 303 is disposed at the bottom of the rectification column 301, and the high temperature refrigerator 303 is used for cooling the liquid phase product output from the rectification column 301.
The cascade refrigerating unit is adopted in the utility model, so that the low-temperature cooling liquefaction of raw material gas is realized, the temperature can be reduced to-50 ℃ to-60 ℃, most of carbon dioxide can be liquefied by combining the compression pressure of multi-stage compression, and further, the carbon dioxide liquid with high purity and high yield can be obtained in the rectifying component 300. Further, the cascade refrigerating unit is characterized in that the low-temperature refrigerator 302 and the high-temperature refrigerator 303 are respectively utilized, namely, two different levels of cold sources of the low-temperature refrigerator 302 and the high-temperature refrigerator 303 are utilized, the low-temperature refrigerator 302 is used as a cold source for liquefying carbon dioxide, the high-temperature refrigerator 303 is used as a supercooling cold source for rectifying the liquid-phase carbon dioxide product of the component 300, and the two cold sources are organically combined to serve each other in the operation process.
In some embodiments, the gas input end of the cryocooler is provided with a recuperation heat exchanger 400, and the dry gas output by the drying assembly 200 enters the heat source pipeline of the recuperation heat exchanger 400 as a heat source.
In some embodiments, the recuperation heat exchanger 400 includes at least two heat exchange chambers 401, and the gas phase product of the rectifying tower 301 sequentially enters each heat exchange chamber 401 to exchange heat and raise temperature.
In the utility model, the dryer is used as a heat source of the reheating heat exchanger 400, so that the non-condensable gas at the top of the rectifying component 300 is heated, and the energy utilization is realized.
In some embodiments, the gas line between adjacent heat exchange chambers 401 is provided with a pressure reducer for reducing the pressure of the warmed gas phase product, such as the second pressure reducer 402 in fig. 4, which may be a pressure reducing valve, for example. According to the utility model, the non-condensable gas at the top of the rectifying tower 301 is subjected to decompression and heat exchange, and does not contain moisture under the condition of maintaining a certain pressure, namely, the non-condensable gas discharged from the top of the rectifying tower is also dry gas.
In one embodiment, a method for capturing carbon by using the carbon capturing device is provided, which comprises the following steps:
the raw gas enters a first-stage compressor 101 for compression, enters a first-stage cooler 103 for cooling and liquefying, a first-stage gas-liquid separator 104 decompresses and returns a liquid product to the first-stage compressor 101, a gas-phase product enters a second-stage compressor 102, enters a second-stage cooler 105 for liquefying after compression, and enters a drying assembly 200 after separation by a second-stage gas-liquid separator 106, and the gas is shunted by a first branch pipeline 204 and a second branch pipeline 205;
in the drying assembly 200, the first dryer 201 is in an adsorption drying state, i.e. the drying air inlet pipe 206 and the drying air outlet pipe 207 of the first dryer 201 are both opened, and the rest of the pipelines are closed; the second dryer 202 is in a regeneration state, namely, a regeneration air inlet pipe 210 and a regeneration air outlet pipe 211 of the second dryer 202 are opened, and other pipelines are closed; the third dryer 203 is in a back-blowing pre-drying state, namely, a back-blowing air inlet pipe 208 and a back-blowing air outlet pipe 209 of the third dryer 203 are opened, and other pipelines are closed;
the gas entering the first branch pipeline 204 enters the third dryer 203 from a back blowing air inlet of the third dryer 203 to be back-blown and pre-dried, and enters a regeneration gas heater 212 to be heated to form regeneration gas, the regeneration gas enters a regeneration gas inlet pipe of the second dryer 202 to regenerate the second dryer 202, and the regenerated gas is sequentially cooled, liquefied and separated into liquid and flows back to the second branch pipeline 205;
the gas in the second branch pipeline 205 enters the first dryer 201 from the drying air inlet pipe 206 of the first dryer 201 to be adsorbed and dried;
the gas after adsorption drying enters a heat source pipeline of the reheating heat exchanger 400 to be used as a heat source for heat exchange, the gas after heat exchange enters a rectifying tower 301 for rectification after being cooled and liquefied by a low-temperature refrigerator 302, a liquid-phase carbon dioxide product is generated at the bottom of the rectifying tower and is collected for use after being supercooled by a high-temperature refrigerator 303, and the non-condensable gas at the top of the tower enters a heat exchange cavity 401 of the reheating heat exchanger 400 to be used after heat exchange and temperature rise, and is collected for use after pressure reduction;
when the adsorption drying effect of the first dryer 201 is reduced, the valve assembly is adjusted to switch the operation state of the dryer, that is, the first dryer 201 is switched to the back-blowing pre-drying state, the second dryer 202 is switched to the adsorption drying state, the third dryer 203 is switched to the regeneration state, the pipeline valves of the corresponding dryers are adjusted to be opened and closed, and for example, a single dryer is taken as an example, the state switching sequence of the single dryer is adsorption drying, back-blowing pre-drying and regeneration, and the single dryer is recycled.
According to a specific embodiment, the compression assembly 100, the drying assembly 200, the rectifying assembly 300 and the regulating valve assembly are adopted to sequentially compress, dry and rectify the raw material gas, the carbon dioxide in the raw material gas is liquefied, and then high-purity carbon dioxide is obtained in the rectifying assembly 300, in addition, three dryers which are alternatively started are adopted in the drying assembly 200, so that the three dryers respectively perform adsorption drying, back blowing and regeneration, continuous drying is realized, and the method has the characteristics of high efficiency, continuity, high purity and the like.
The above examples illustrate only a few embodiments of the utility model, which are described in detail and are not to be construed as limiting the scope of the utility model. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the utility model, which are all within the scope of the utility model. The scope of the utility model is therefore intended to be covered by the appended claims, and the description and drawings may be interpreted in accordance with the contents of the claims.
Claims (10)
1. The utility model provides a carbon capture device, its characterized in that, carbon capture device includes compression subassembly, drying module, rectifying element and governing valve subassembly, compression subassembly, drying module and rectifying element set gradually along raw materials gas flow direction:
a compression assembly for pressurizing the feed gas;
the drying assembly comprises three dryers which are sequentially connected, and the dryers are connected with a drying pipeline, a back blowing pipeline and a regeneration pipeline;
the compression assembly is connected with the drying assembly through a connecting main pipe, the output end of the connecting main pipe is connected with a first branch pipeline and a second branch pipeline in parallel, the first branch pipeline is respectively connected with the input end of the back blowing pipeline of each dryer, and the second branch pipeline is respectively connected with the input end of the drying pipeline of each dryer;
the drying pipeline, the back flushing pipeline and the regeneration pipeline in the dryer are respectively and independently started, and the starting states of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer are different and are alternatively started;
the drying assembly further comprises a regeneration gas heater and cooling dehydrators, wherein the output ends of the back blowing pipelines in the dryers are connected with the regeneration gas heater, the regeneration gas heater is used for heating the back-blown gas, the output ends of the regeneration gas heater are respectively connected with the input ends of the regeneration pipelines in the dryers, the output ends of the regeneration pipelines in the dryers are connected with the cooling dehydrators, the cooling dehydrators are used for cooling liquid in liquefied removal gas, and the gas output ends of the cooling dehydrators are connected with the second branch pipeline;
the regulating valve assembly comprises a control valve arranged on a pipeline of the drying assembly and is used for switching the closing and starting of the drying pipeline, the back flushing pipeline and the regeneration pipeline in each dryer;
and the rectification component is used for rectifying and purifying the dry gas output by the drying component.
2. The carbon capture apparatus of claim 1, wherein in the drying assembly, the drying line comprises a drying air inlet pipe connected to the top of the dryer and a drying air outlet pipe connected to the bottom of the dryer, the blowback line comprises a blowback air inlet pipe connected to the bottom of the dryer and a blowback air outlet pipe connected to the top of the dryer, and the regeneration line comprises a regeneration air inlet pipe connected to the bottom of the dryer and a regeneration air outlet pipe connected to the top of the dryer;
the first branch pipelines are respectively and independently connected with the back blowing air inlet pipes of the dryers, and the second branch pipelines are respectively and independently connected with the drying air inlet pipes of the dryers;
the back-blowing air outlet pipes of the dryers are all connected with the regenerated gas heater, the air outlet ends of the regenerated gas heater are respectively and independently connected with the regenerated air inlet pipes of the dryers, the regenerated air outlet pipes of the dryers are all connected with the cooling dehydrator, and the gas phase output ends of the cooling dehydrator are connected with the second branch pipeline.
3. The carbon capture apparatus of claim 1, wherein the compression assembly comprises at least two compressors, the output ends of the compressors each being provided with a cooler and a gas-liquid separator connected in sequence.
4. The carbon capture apparatus of claim 1, wherein the compression assembly comprises a first stage compressor and a second stage compressor along the flow direction of the feed gas, wherein the output end of the first stage compressor and the output end of the second stage compressor are respectively provided with a cooler and a gas-liquid separator in sequence;
the gas-liquid separator at the output end of the first-stage compressor is connected to the input end of the first-stage compressor through a liquid circulation pipeline, and the liquid circulation pipeline is connected with the liquid phase output end of the gas-liquid separator;
the liquid circulation pipeline is provided with a pressure reducer.
5. The carbon capture apparatus of claim 1, wherein the cooling water trap comprises a regeneration gas cooler and a regeneration gas knockout vessel connected in sequence.
6. The carbon capture apparatus of any one of claims 1-5, wherein an cascade refrigeration unit is disposed between the rectifying assembly and the drying assembly, the cascade refrigeration unit comprising a cryocooler and a cryocooler, the cryocooler configured to cool and liquefy dry gas entering the rectifying assembly.
7. The carbon capture apparatus of claim 6, wherein the rectification assembly comprises a rectification column, the bottom of the rectification column being provided with the high temperature refrigerator for cooling liquid phase products output from the rectification column.
8. The carbon capture apparatus of claim 7, wherein the cryogenic refrigerator is provided with a reheat heat exchanger at a gas input end thereof, and wherein the dry gas output by the drying assembly enters a heat source pipeline of the reheat heat exchanger as a heat source.
9. The carbon capture apparatus of claim 8, wherein the recuperative heat exchanger comprises at least two stages of heat exchange chambers, and the vapor phase product of the rectifying column sequentially enters each of the heat exchange chambers to exchange heat and raise temperature.
10. The carbon capture apparatus of claim 9, wherein gas lines between adjacent heat exchange chambers are provided with pressure reducers for depressurizing the warmed gas phase products.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320080590.8U CN219907006U (en) | 2023-01-12 | 2023-01-12 | Carbon trapping device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320080590.8U CN219907006U (en) | 2023-01-12 | 2023-01-12 | Carbon trapping device |
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| CN219907006U true CN219907006U (en) | 2023-10-27 |
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| CN202320080590.8U Active CN219907006U (en) | 2023-01-12 | 2023-01-12 | Carbon trapping device |
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| CN (1) | CN219907006U (en) |
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2023
- 2023-01-12 CN CN202320080590.8U patent/CN219907006U/en active Active
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