WO2025200538A1 - 一种吸附器、吸附系统及吸附方法 - Google Patents

一种吸附器、吸附系统及吸附方法

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Publication number
WO2025200538A1
WO2025200538A1 PCT/CN2024/136128 CN2024136128W WO2025200538A1 WO 2025200538 A1 WO2025200538 A1 WO 2025200538A1 CN 2024136128 W CN2024136128 W CN 2024136128W WO 2025200538 A1 WO2025200538 A1 WO 2025200538A1
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WO
WIPO (PCT)
Prior art keywords
gas
adsorption
adsorber
air
outlet
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/CN2024/136128
Other languages
English (en)
French (fr)
Inventor
周爱国
郑家乐
孔繁鑫
杨川箬
魏炜
陈进富
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China National Petroleum Corp
CNPC Research Institute of Safety and Environmental Technology Co Ltd
Original Assignee
China National Petroleum Corp
CNPC Research Institute of Safety and Environmental Technology Co Ltd
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Filing date
Publication date
Application filed by China National Petroleum Corp, CNPC Research Institute of Safety and Environmental Technology Co Ltd filed Critical China National Petroleum Corp
Publication of WO2025200538A1 publication Critical patent/WO2025200538A1/zh
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0423—Beds in columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/20—Organic adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/404—Further details for adsorption processes and devices using four beds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • DAC Direct Air Capture
  • the present application provides an adsorption method for the above adsorber, which is simple to operate, improves adsorption and desorption efficiency, and reduces operating costs.
  • the present application also provides an adsorption system comprising the above adsorber, which reduces system pressure drop and improves adsorption and desorption efficiency.
  • the interval between two adjacent adsorption beds forms a channel, the channel is connected to the air inlet and the air outlet respectively, and the width of the channel gradually decreases in the direction of the air inlet and the air outlet;
  • the aperture of the airflow distribution plate decreases gradually from the inlet to the outlet of the airflow distribution plate.
  • a plurality of adsorption beds are spaced apart in the axial or radial direction of the shell; wherein,
  • At least one of the air inlets is provided on the housing corresponding to the channel; and/or,
  • At least one of the air outlets is provided on the housing corresponding to the channel.
  • the channel corresponding to the air inlet is different from the channel corresponding to the air outlet; and/or,
  • a partition is provided in the middle of the channel corresponding to the air inlet.
  • the thickness of the adsorption bed is 1-20 cm; and/or,
  • the thickness of the airflow distribution plate is 2-5 mm; and/or,
  • the ratio of the aperture at the outlet of the airflow uniform distribution plate to the aperture at the inlet of the airflow uniform distribution plate is 1:(2-5).
  • the ratio of the width of the channel to the thickness of the adsorption bed is 1:(2-10).
  • the shell is further provided with a liquid outlet, which is used to discharge the condensate in the adsorption bed; and/or,
  • the outer side of the shell is also covered with a heat-insulating layer.
  • the present application provides an adsorption method of the adsorber described above, comprising the following steps:
  • the gas to be adsorbed is sent to the cavity in the adsorber through the air inlet, dispersed by the air flow distribution plate, and then enters the adsorption bed for adsorption treatment to obtain adsorbed gas and a saturated adsorption bed, and the adsorbed gas is extracted through the air outlet;
  • the adsorbent has a particle size distribution of 0.3 mm to 1.5 mm, and the adsorbent comprises a solid amine adsorption material; and/or,
  • step (3) the regeneration gas is water vapor, the temperature of the regeneration treatment is 80-120° C., and the time is 10-30 minutes; the regeneration treatment includes steam direct purge regeneration treatment.
  • the present application provides an adsorption system comprising the adsorber described above.
  • it also includes a gas purification and cooling device for adsorbed gas, an adsorption device, a regeneration gas generating device, and a separation device;
  • the adsorption device comprises at least one adsorber
  • FIG1 is a schematic diagram of the adsorber structure in a specific embodiment of the present application.
  • FIG3 is a schematic diagram of an adsorption system in a specific embodiment of the present application.
  • FIG4 is a schematic diagram of an adsorption system in a specific embodiment of the present application.
  • Figure 5 shows the change of CO2 concentration at the adsorption outlet with adsorption time
  • Figure 6 shows the change of CO2 adsorption capacity at the adsorption outlet versus adsorption time
  • FIG7 is a comparison chart of regeneration rates of different regeneration treatment methods
  • Figure 8 is a graph showing the change in adsorption capacity at different temperatures
  • FIG9 is a graph showing pressure changes over time during vacuum treatment
  • FIG10 shows the temperature change over time during the cooling process.
  • FIG1 is a schematic diagram of the adsorber structure in a specific embodiment of the present application.
  • the adsorber comprises a shell 1 having a cavity therein, and a plurality of adsorption beds 4 arranged at intervals in the cavity, and a plurality of air flow distribution plates 6.
  • the shell 1 is further provided with a plurality of air inlets 7 and air outlets 8.
  • the air inlets 7 are used to inject the gas to be adsorbed and the regeneration gas into the cavity, respectively, and the air outlets 8 are used to output the adsorbed gas and the desorbed gas.
  • the gap between two adjacent adsorption beds 4 forms a channel, which is connected to the air inlet 7 and the air outlet 8 respectively, and the width of the channel gradually decreases in the direction of the air inlet and the air outlet;
  • the aperture of the airflow distribution plate 6 decreases gradually from the inlet to the outlet of the airflow distribution plate 6 .
  • multiple means greater than or equal to two, and the number of “multiple” can be the same or different; this application does not limit the specific form of each part; wherein, the housing 1 with a cavity inside can be circular or square;
  • a plurality of adsorption beds 4 are arranged in the cavity inside the shell 1.
  • the present application does not limit the shape of the adsorption bed 4, which can be rectangular or trapezoidal.
  • the adsorption bed 4 is filled with adsorbent, and the adsorption bed 4 is provided with a supporting layer in the thickness direction.
  • the supporting layer does not penetrate the adsorbent with the smallest particle size and allows the gas to pass smoothly.
  • the supporting layer can be a fabric or a plate-like structure; the airflow enters the plurality of adsorption beds 4 for adsorption or regeneration treatment, thereby improving the adsorption and desorption efficiency.
  • the airflow distribution plate 6 can achieve distribution and collection of airflow.
  • the airflow distribution plate 6 is evenly provided with small holes to evenly distribute the airflow to the adsorption bed, thereby reducing the pressure drop of the bed and avoiding the concentration of airflow in certain areas. At the same time, it plays a role in filtering impurities in the gas to be adsorbed, thereby improving the adsorption and desorption efficiency.
  • the housing 1 is further provided with a plurality of air inlets 7 and air outlets 8, through which gas can simultaneously enter or leave the cavity in the adsorber; the air inlets 7 are used to inject the gas to be adsorbed and the regeneration gas into the cavity, respectively, and the air outlets 8 are used to output the adsorbed gas and the desorbed gas, respectively. It can be understood that when the gas to be adsorbed is injected into the cavity, the adsorbed gas is output; when the regeneration gas is injected into the cavity, the desorbed gas is output;
  • the gap between two adjacent adsorption beds 4 constitutes a channel, which is respectively connected to the air inlet 7 and the air outlet 8.
  • the channel connected to the air inlet 7 is the air inlet channel 12, and the gas enters the adsorption bed 4 through the air inlet channel 12.
  • the channel connected to the air outlet 8 is the air outlet channel 13, and the gas leaves the adsorption bed through the air outlet channel 13.
  • the width of the channel gradually decreases according to the air flow direction of the air inlet and the air outlet.
  • the cross-sectional area of the channel becomes smaller and smaller from near the inlet to far away from the inlet, so that the air flow velocity at the corresponding cross section is kept consistent, and the air flow can effectively utilize the air flow uniformly distributed by the air flow uniformly distributed plate;
  • the air flow After the air flow enters the cavity in the adsorber through the air inlet 7, it flows through the inlet of the air flow distribution plate 6, and is dispersed by the air flow distribution plate. After being dispersed and evenly distributed, the air flow leaves through the outlet of the air flow distribution plate and enters the adsorption bed 4; the aperture of the air flow distribution plate 6 gradually decreases from the inlet to the outlet of the air flow distribution plate 6, forming a frustum shape, which can effectively distribute the air flow, reduce the air flow resistance and thus reduce the bed pressure drop;
  • the adsorber provided in the present application cooperates with each other through the spaced arrangement of multiple adsorption beds, multiple air inlets and outlets, and specially structured channels, so that the airflow enters the cavity inside the adsorber through multiple air inlets, and then passes through the airflow distribution plate and the adsorption bed in sequence along the direction of airflow flow, which can reduce the bed pressure drop and improve the adsorption and desorption efficiency.
  • a plurality of adsorption beds 4 are spaced apart in the axial or radial direction of the shell 1 ; wherein at least one air inlet 7 is provided on the shell corresponding to the channel; and at least one air outlet 8 is provided on the shell corresponding to the channel.
  • the present application does not limit the setting direction of the adsorption bed 4.
  • Multiple adsorption beds 4 can be spaced apart in the radial direction of the shell 1 (as shown in Figure 1), or can be spaced apart in the axial direction of the shell 1 (as shown in Figure 2); in one specific embodiment, at least one air inlet 7 is provided on the shell 1 corresponding to the channel, so that the airflow can enter the closed shell 1 through the air inlet 7, and the gas to be adsorbed and the regenerated gas can share one air inlet, or can be further subdivided into two parallel air inlets; in another specific embodiment, at least one air outlet 8 is provided on the shell 1 corresponding to the channel, so that the airflow can leave the closed shell 1 through the air outlet 8, and the adsorbed gas and the desorbed gas can share one air outlet, or can be further subdivided into two parallel air outlets.
  • the channel corresponding to the air inlet 7 is different from the channel corresponding to the air outlet 8 .
  • each channel can and can only be provided with an air inlet or an air outlet, so that the air flow enters the path to leave the adsorber and passes through at least one adsorption bed layer, thereby improving the adsorption and desorption efficiency.
  • a partition 18 is provided in the middle of the channel corresponding to the air inlet
  • adding a partition 18 in the middle of the air inlet channel can evenly divide the gas to be adsorbed into two parts when entering the air inlet channel, which helps to further distribute the airflow, reduce the bed pressure drop and improve the adsorption and regeneration efficiency.
  • the thickness of the adsorption bed 4 is 1-20 cm.
  • the thickness of the adsorption bed refers to the average path length of the airflow through the adsorption bed. It can be understood that the thickness of the adsorption bed is closely related to the resistance encountered by the airflow penetrating therethrough. The applicant has found that when the thickness of the adsorption bed 4 is 1-20 cm, the adsorption and desorption efficiency can be guaranteed while further reducing the bed pressure drop and improving the mass transfer efficiency.
  • the thickness of the airflow distribution plate is 2-5 mm; the ratio of the aperture at the outlet of the airflow distribution plate to the aperture at the inlet of the airflow distribution plate is 1:(2-5);
  • the air flow uniform distribution plate is a plate-like structure with a certain thickness and distributed small holes. Since the aperture gradually decreases from the inlet to the outlet, it is truncated into a cone shape.
  • the applicant has found through research that when the thickness of the air flow uniform distribution plate is 2-5 mm and the ratio of the aperture at the outlet of the air flow uniform distribution plate to the aperture at the inlet of the air flow uniform distribution plate is 1: (2-5), the air flow resistance can be further reduced, the air flow can be evenly distributed, and the bed pressure drop can be further reduced.
  • the ratio of the width of the channel to the thickness of the adsorption bed 4 is 1:(2-10).
  • the width of the channel refers to the average width.
  • the applicant has found that when the ratio of the channel width to the thickness of the adsorption bed is 1:(2-10), it is more conducive to the airflow to efficiently pass through the adsorption bed, reduce the bed pressure drop, and improve the mass transfer efficiency.
  • a pressure monitoring gauge 5 is further provided, and the pressure monitoring gauge 5 is used to monitor the pressure of the first end surface 2 and the second end surface 3 that are arranged opposite to each other in the thickness direction of the adsorption bed 4;
  • the present application does not limit the specific setting method of the pressure detection gauge 5. It can be set on the shell 1 or not. Any method that can monitor and output the pressure of the first end face 2 and the second end face 3 of the adsorption bed 4 that are relatively set in the thickness direction can be used.
  • a temperature monitoring meter 9 is further provided, and the temperature monitoring meter 9 is used to monitor the temperature of the first end surface 2 and the second end surface 3 of the adsorption bed 4 which are arranged opposite to each other in the thickness direction;
  • the present application does not limit the specific setting method of the temperature monitoring meter 9. It can be set on the shell 1 or not. Any method that can monitor and output the temperatures of the first end face 2 and the second end face 3 of the adsorption bed 4 that are relatively set in the thickness direction can be used.
  • the housing 1 is further provided with a liquid outlet 10, which is used to discharge the condensate in the adsorption bed 4;
  • condensate may be generated during the adsorption or desorption process, so a liquid outlet 10 is provided on the shell 1 to discharge the condensate in the adsorption bed 4 and the shell 1, thereby further improving the mass transfer efficiency and reducing the bed pressure drop.
  • the outer side of the shell 1 is also covered with an insulation layer; by providing the insulation layer on the outer side of the shell 1, it is beneficial to keep the temperature inside the adsorber constant, further improve the adsorption and desorption efficiency, and maintain the reaction stability.
  • the shell 1 is also provided with an adsorbent filling inlet 16 and an adsorbent replacement outlet 17.
  • the adsorbent filler is first naturally filled into the upper part of the adsorption bed 4 through the adsorbent filling inlet 16, and then pressurized air is used for auxiliary filling; when the adsorbent needs to be replaced, the adsorbent filler is discharged and replaced through the adsorbent replacement outlet 17; a vent pipe 11 is also provided on the upper part of the shell 1, which helps to adjust the pressure inside the adsorber, etc.
  • the present application also provides an adsorption method of the above adsorber, comprising the following steps:
  • the gas to be adsorbed is sent to the cavity in the adsorber through the air inlet, dispersed by the air flow distribution plate, and then enters the adsorption bed for adsorption treatment to obtain adsorbed gas and a saturated adsorption bed.
  • the adsorbed gas is extracted through the air outlet;
  • the regenerated gas is sent to the cavity in the adsorber through the air inlet, and after being dispersed by the air flow distribution plate, the saturated adsorption bed is regenerated to obtain desorbed gas, condensate and regenerated adsorption bed; the desorbed gas is collected through the air outlet;
  • the adsorption method provided in the present application is applicable to any treatment that directly utilizes a solid adsorbent to adsorb a gas; specifically, in step (1), the gas to be adsorbed is sent to the cavity in the adsorber through the air inlet, and after being dispersed by the air flow uniform distribution plate, enters the adsorption bed for adsorption treatment to remove the components to be adsorbed in the gas to be adsorbed; it can be understood that the adsorber is also provided with a gas analyzer at the air inlet and the air outlet, respectively, for detecting the concentration of the components to be adsorbed in the gas to be adsorbed, and obtaining the inlet concentration and the outlet concentration respectively.
  • step (2) the remaining gas in the adsorber is vacuumed until the pressure in the adsorber is -85kPa to -95kPa; this is beneficial to improving regeneration efficiency and reducing costs;
  • step (3) the regenerated gas is sent to the cavity in the adsorber through the air inlet, and after being dispersed by the air flow uniform distribution plate, the saturated adsorption bed is regenerated to desorb the components to be adsorbed that are enriched in the saturated adsorption bed.
  • the air outlet of the adsorber is also connected to a separation device, a gas analyzer, etc., for separating and detecting the flow rate of the desorbed gas. When the flow rate of the desorbed gas is detected to be 0 L/min, it indicates that all the components to be adsorbed in the adsorption bed have been desorbed.
  • step (4) the regenerated adsorption bed is cooled, which is beneficial to improving the efficiency of the next adsorption treatment; steps (1) to (4) are one cycle of the adsorption method provided in this application, and step (1) is directly performed after step (4) to start the next round of adsorption treatment.
  • the adsorption method of the adsorber provided in the present application is simple and easy to implement, which is beneficial to reducing the bed pressure drop and improving the mass transfer efficiency of the gas.
  • the adsorption bed can be regenerated indefinitely, and the treatment process does not consume auxiliary materials, thereby improving the adsorption and regeneration efficiency and helping to reduce operating costs.
  • the adsorption bed includes an adsorbent, and the ratio of the mass of the adsorbent to the adsorption amount of carbon dioxide is 0.9-2 mmol/g; the particle size distribution of the adsorbent is 0.3 mm to 1.5 mm, and the adsorbent includes a solid amine adsorption material; in step (1), the flow rate of the gas to be adsorbed is 200-300 Nm 3 /h; the temperature of the adsorption treatment is 20-40° C. and the time is 100-120 minutes; in step (3), the regeneration gas is water vapor, the temperature of the regeneration treatment is 80-120° C., and the time is 10-30 minutes; the regeneration treatment includes steam direct purge regeneration treatment.
  • the gas to be adsorbed is air
  • the component to be adsorbed and the desorbed gas are carbon dioxide.
  • the ratio of the mass of the adsorbent to the amount of carbon dioxide adsorbed is 0.9-2 mmol/g
  • the particle size distribution of the adsorbent is 0.3 mm to 1.5 mm
  • the adsorbent comprises a solid amine adsorption material, specifically, an amine-functionalized solid amine adsorption material grafted with amino functional groups
  • the amount of gas to be adsorbed is 200-300 Nm 3 /h
  • the temperature of the adsorption treatment is 20-40°C and the time is 100-120 min
  • the regeneration gas is water vapor, the temperature of the regeneration treatment is 80-120°C and the time is 10-30 min
  • the regeneration treatment includes a steam direct purge regeneration treatment; under the above parameters, it is beneficial to further improve the capture efficiency of the adsor
  • the present application also provides an adsorption system, comprising the adsorber described above.
  • the adsorption system including the above adsorber can reduce the bed pressure drop of the gas in the adsorber, improve the adsorption and regeneration efficiency, and reduce the operating cost.
  • FIG3 is a schematic diagram of an adsorption system in a specific embodiment of the present application. As shown in FIG3 , it further includes a gas purification and cooling device C1 to be adsorbed, an adsorption device T1, a regeneration gas generating device K1, and a separation device F1;
  • the adsorption device T1 includes at least one adsorber
  • the outlet of the adsorbed gas purification cooling device C1 is connected to the air inlet of the adsorber, and the air outlet of the adsorber is used to output the adsorbed gas;
  • the outlet of the regeneration gas generator K1 is connected to the air inlet of the adsorber, and the air outlet of the adsorber is also connected to the inlet of the separation device F1.
  • the gas phase outlet of the separation device F1 is used to output product gas, and the liquid phase outlet of the separation device F1 is connected to the reflux port of the regeneration gas generator K1.
  • the adsorbed gas purification and cooling device C1 can filter impurities in the adsorbed gas and reduce its temperature;
  • the adsorption device T1 includes at least one of the above-mentioned adsorbers, and the adsorbers can be connected in parallel or in series;
  • the regeneration gas generating device K1 can generate regeneration gas; and
  • the separation device F1 can separate the adsorbed components in the desorbed gas from the regeneration gas.
  • the inlet of the gas purification cooling device C1 to be adsorbed is the inlet of the adsorption system.
  • the gas to be adsorbed enters the gas purification cooling device C1 through the inlet of the gas purification cooling device C1, is filtered, purified and cooled, leaves through the outlet of the gas purification cooling device C1, and enters the adsorption device T1 through the air inlet of the adsorber, where it is adsorbed.
  • the adsorbed gas and the saturated adsorption bed are obtained; the adsorbed gas is extracted through the air outlet of the adsorber and leaves the adsorption system; the outlet of the regeneration gas generating device K1 is also connected to the air inlet of the adsorber.
  • the regenerated gas is produced through the outlet of the regeneration gas generator K1 and enters the adsorber through the air inlet of the adsorber to regenerate the saturated adsorption bed, desorbing the components to be adsorbed in the saturated adsorption bed to obtain a regenerated adsorption bed and desorbed gas.
  • the desorbed gas is produced through the air outlet of the adsorber and enters the separation device F1 through the inlet of the separation device F1, where the components to be adsorbed are separated from the regenerated gas to obtain desorbed gas and regeneration circulating liquid.
  • the desorbed gas leaves through the gas phase outlet of the separation device F1 and outputs product gas.
  • the regeneration circulating liquid is connected to the reflux port of the regeneration gas generator K1 to recover the regenerated gas.
  • FIG4 is a schematic diagram of an adsorption system in a specific embodiment of the present application.
  • the regeneration gas generating device when the adsorption system is used to directly capture carbon dioxide from air, the regeneration gas generating device includes a steam generator K01 and a flow regulating unit K02.
  • the steam generator K01 is used to heat the room temperature supply water to boiling and generate sufficient steam for heating the adsorbent.
  • the flow regulating unit K02 mainly includes an opening regulating valve and a flow meter, and adjusts the steam flow rate through a PID control system.
  • the adsorption device includes four parallel-connected adsorbers T01-T04, vacuum equipment T05, blower T06, online infrared gas analyzer T07, automatic control system and instrument T08, etc.
  • the vacuum equipment T05 is used to extract the remaining air in the adsorber and promptly extract the residual gas during the desorption and regeneration process to accelerate the adsorption and regeneration efficiency
  • the blower T06 is used to pass air into the adsorber and overcome sufficient resistance along the way
  • the online infrared gas analyzer T07 is used to detect concentration changes at the air inlet and outlet of the adsorber in real time
  • the automatic control system and instrument T08 are used to timely adjust the flow rate, and all valves are connected to the programmable logic controller (PLC), which controls the operation of the entire system.
  • PLC programmable logic controller
  • the adsorption system also includes a steam boiler softened water treatment unit K03, which is used to treat the discharged liquid from the condensation section at the bottom of the adsorption tower; specifically, the liquid outlet of the adsorber and the liquid phase outlet of the gas-liquid separator are respectively connected to the inlet of the steam boiler softened water treatment unit, and the outlet of the steam boiler softened water treatment unit is connected to the reflux port of the steam generator.
  • a steam boiler softened water treatment unit K03 which is used to treat the discharged liquid from the condensation section at the bottom of the adsorption tower; specifically, the liquid outlet of the adsorber and the liquid phase outlet of the gas-liquid separator are respectively connected to the inlet of the steam boiler softened water treatment unit, and the outlet of the steam boiler softened water treatment unit is connected to the reflux port of the steam generator.
  • This embodiment uses an adsorber as shown in FIG1 , wherein four adsorption beds are spaced apart in the axial direction, the number of air inlets is two, the number of air outlets is three, and the number of uniform distribution plates is four; the thickness of the adsorption bed is 10 cm; the ratio of the width of the channel to the thickness of the adsorption bed is 1:2; the thickness of the air flow uniform distribution plate is 3 mm; and the ratio of the aperture at the outlet of the air flow uniform distribution plate to the aperture at the inlet of the air flow uniform distribution plate is 1:3;
  • This embodiment performs adsorption treatment on carbon dioxide in the air, where the concentration of carbon dioxide in the air is 400 ppm, and includes the following steps:
  • Air is sent to the cavity in the adsorber through the air inlet at an air flow rate of 260 Nm 3 /h. After being dispersed by the air flow distribution plate, the air enters the adsorption bed for adsorption treatment.
  • the adsorbent provided in the adsorption bed is a solid amine adsorption material with amine functionalized grafted amino functional groups, and its particle size is 0.6 mm.
  • the adsorption treatment temperature is 20°C and the time is 120 minutes. The adsorbed air and the saturated adsorption bed are obtained, and the adsorbed air is collected through the air outlet;
  • Air is introduced to cool the regenerated adsorption bed.
  • the cooling temperature is the ambient temperature and the cooling time is 10 minutes.
  • step (1) the adsorption treatment time is 60 minutes.
  • step (1) the adsorption treatment time is 180 minutes.
  • step (1) the adsorption treatment temperature is 10°C.
  • step (3) the regeneration process uses steam-assisted heat exchange.
  • an adsorber as shown in Figure 2 is used, wherein four adsorption beds are spaced apart in the axial direction, the number of air inlets is 2, the number of air outlets is 2, and the number of uniform distribution plates is 2; the thickness of the adsorption bed is 10 cm; and the ratio of the channel width to the thickness of the adsorption bed is 1:2.
  • the difference between this embodiment and embodiment 1 is that the thickness of the adsorption bed is 20 cm.
  • Example 1 The difference between this comparative example and Example 1 is that: the number of adsorption beds is 1, the number of air inlets is 1, the number of air outlets is 1 and the number of uniform distribution plates is 1; the thickness of the adsorption bed is 40 cm.
  • Figure 5 shows the change of CO2 concentration at the adsorption outlet with adsorption time, where Figures 1, 3-6 are repeated tests with an adsorption time of 60 minutes, Figure 2 is an adsorption time of 180 minutes, and Figures 7-10 are repeated tests with an adsorption time of 120 minutes.
  • Figure 6 shows the change of CO2 adsorption capacity at the adsorption outlet with adsorption time. As can be seen from the figure, when the adsorption time is 60 minutes, the adsorption capacity is 0.88 to 1.1 mmol/g; when the adsorption time is 120 minutes, the adsorption capacity is 1.35 to 1.62 mmol/g.
  • Example 1 and Example 4 The air after adsorption in Example 1 and Example 4 was detected by an online infrared gas analyzer, and the temperature of the adsorption bed during the adsorption process was detected by a temperature monitoring meter, and FIG8 was obtained.
  • Figure 8 is a graph showing the change in adsorption capacity at different temperatures.
  • the average temperature of the adsorption process is 35-40°C, and the average adsorption capacity for 60 min is about 0.65 mmol/g; in Example 1, the average temperature of the adsorption process is 15-20°C, and the average adsorption capacity for 60 min is about 0.97 mmol/g. It can be seen that a lower adsorption temperature is conducive to the adsorption process. Therefore, when the adsorption temperature is 10-20°C, it is more conducive to ensuring efficient adsorption.
  • Example 1 The temperature change of the adsorption bed during the cooling process in step (4) of Example 1 was tested using a temperature monitoring meter. The results are shown in FIG10 .
  • Figure 10 shows the temperature change over time during the cooling process.
  • Using air cooling can reduce the bed temperature to room temperature in about 10 minutes, which improves the cooling efficiency, reduces the energy consumption of the regeneration process, greatly reduces the adsorber regeneration cooling operation time and shortens the adsorption/desorption cycle time.

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Abstract

本申请提供一种吸附器，包括内部具有空腔的壳体，以及位于空腔中的多个间隔设置的吸附床层、多个气流均布板，壳体还设置有多个进气口和出气口，进气口用于分别向空腔内注入待吸附气和再生气，出气口用于输出吸附后气体和解吸气体；相邻的两个吸附床层之间的间隔构成通道，通道分别与进气口和出气口连通，且通道的宽度按照进气口、出气口的方向逐渐增大减小；多个气流均布板的入口均与进气口连通，气流均布板的出口朝向吸附床层；气流均布板的入口到气流均布板的出口孔径逐渐减小；用以降低床层压降，并且提高吸附和解吸效率。

Description

一种吸附器、吸附系统及吸附方法
本申请要求于2024年3月25日提交中国专利局、申请号为CN 202410346473.0、申请名称为“一种吸附器、吸附系统及吸附方法”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请属于直接空气捕集二氧化碳技术领域，具体涉及一种吸附器、空气直接捕集系统及吸附方法。
背景技术
随着全球温室气体排放不断增加，气候变化成为全球性问题。许多地区已经承诺在未来几十年内实现净零排放或碳中和目标。空气直接捕集二氧化碳(Direct Air Capture，DAC)技术为实现这些目标提供了一种有效的手段，旨在从大气中移除二氧化碳，从而有助于减缓气候变化和减少温室气体排放。尽管DAC技术具有减缓气候变化的巨大潜力，但要实现其广泛应用，需要解决一系列挑战和瓶颈。
应用DAC技术涉及到建造大型吸附器和相关基础设施，大型吸附器一直向着大型化、低能耗化发展；立式径向流吸附器的出现，有效解决了立式轴向吸附器和卧式垂直流吸附器的占地面积大、分子筛床层难平整等问题。而如今，由于空气处理量的进一步增大，空气中的二氧化碳浓度很低，因此，对于高通量、低浓度的空气直接捕集二氧化碳系统普遍存在系统压降高、吸附和再生效率低等问题。
发明内容
本申请提供了一种吸附器，用于解决现有技术中的吸附处理高通量、低浓度的气体组分时存在的系统压降高、吸附和解吸效率低等问题。
本申请提供了一种上述吸附器的吸附方法，操作简单，提高了吸附和解吸效率，降低了运行成本。
本申请还提供一种包括上述吸附器的吸附系统，降低系统压降，提高吸附和解吸效率。
一方面，本申请提供一种吸附器，包括内部具有空腔的壳体，以及位于所述空腔中的多个间隔设置的吸附床层、多个气流均布板，所述壳体还设置有多个进气口和出气口，所述进气口用于分别向所述空腔内注入待吸附气和再生气，所述出气口用于输出吸附后气体和解吸气体；
相邻的两个所述吸附床层之间的间隔构成通道，所述通道分别与所述进气口和出气口连通，且所述通道的宽度按照进气口、出气口的方向逐渐减小；
多个所述气流均布板的入口均与所述进气口连通，所述气流均布板的出口朝向所述吸附床层；
所述气流均布板的入口到所述气流均布板的出口孔径逐渐减小。
进一步地，多个所述吸附床层在所述壳体的轴向或径向方向上间隔设置；其中，
至少一个所述进气口设置在与所述通道对应的壳体上；和/或，
至少一个所述出气口设置在与所述通道对应的壳体上。
进一步地，与所述进气口对应的通道和与所述出气口对应的通道不同；和/或，
与所述进气口对应的通道中间设置有隔板。
进一步地，所述吸附床层的厚度为1-20cm；和/或，
所述气流均布板的厚度为2-5mm；和/或，
所述气流均布板的出口处孔径与所述气流均布板入口处孔径之比为1：(2-5)。
进一步地，所述通道的宽度与所述吸附床层的厚度比为1：(2-10)。
进一步地，还设置有压力监测表，所述压力检测表用于监测所述吸附床层在厚度方向上相对设置的第一端面和第二端面的压力；和/或，
还设置有温度监测表，所述温度检测表用于监测所述吸附床层在厚度方向上相对设置的第一端面和第二端面的温度；和/或，
壳体还设置有出液口，所述出液口用于排出所述吸附床层中的冷凝液；和/或，
所述壳体外侧还包覆设置保温层。
另一方面，本申请提供一种上述的吸附器的吸附方法，包括以下步骤：
(1)将待吸附气通过进气口送至所述吸附器中的空腔，通过气流均布板的分散处理后，进入吸附床层进行吸附处理，得到吸附后气体和饱和吸附床层，所述吸附后气体经出气口采出；
(2)对所述吸附器内剩余气体进行抽真空处理，直到所述吸附器内压力为-85kPa～-95kPa；
(3)将再生气通过所述进气口送至所述吸附器中的空腔，通过所述气流均布板的分散处理后，对所述饱和吸附床层进行再生处理，得到解吸气体、冷凝液和再生吸附床层；所述解吸气体经所述出气口采出；
(4)对所述再生吸附床层进行冷却处理。
进一步地，当所述待吸附气为空气、所述解吸气体为二氧化碳时，所述吸附床层包括吸附剂，所述吸附剂的质量与所述二氧化碳的吸附量之比为0.9-2mmol/g；和/或，
所述吸附剂的粒径分布为0.3mm～1.5mm，所述吸附剂包括固态胺吸附材料；和/或，
步骤(1)中，所述待吸附气的通入量为200-300Nm3/h；所述吸附处理的温度为20-40℃、时间为100-120min；和/或，
步骤(3)中，所述再生气为水蒸汽，所述再生处理的温度为80-120℃、时间为10-30min；所述再生处理包括蒸汽直接吹扫再生处理。
再一方面，本申请提供一种吸附系统，包括上述的吸附器。
进一步地，还包括待吸附气净化冷却装置、吸附装置、再生气发生装置、分离装置；
其中，所述吸附装置包括至少一个所述吸附器；
所述待吸附气净化冷却装置的出口与所述吸附器的进气口连通，所述吸附器的出气口用于输出吸附后气体；
所述再生气发生装置的出口与所述吸附器的进气口连通，所述吸附器的出气口还与所述分离装置的入口连通，所述分离装置的气相出口用于输出产品气，所述分离装置的液相出口与所述再生气发生装置的回流口连通。
本申请提供一种吸附器，通过多个吸附床层的间隔设置、多个进气口和出气口以及特殊结构的通道相互配合，使气流通过多个进气口进入吸附器内的空腔后，沿着气流流动方向依次经过气流均布板和吸附床层，可以降低床层压降，并且提高吸附和解吸效率。
附图说明
图1为本申请一具体实施方式中的吸附器结构示意图；
图2为本申请一具体实施方式中的吸附器结构示意图；
图3为本申请一具体实施方式中的吸附系统示意图；
图4为本申请一具体实施方式中的吸附系统示意图；
图5为吸附出口CO2浓度随吸附时间变化图；
图6为吸附出口CO2吸附量随吸附时间变化图；
图7为不同再生处理方式的再生速率对比图；
图8为不同温度下的吸附量变化图；
图9为抽真空处理中压力随时间变化图；
图10为冷却处理中温度随时间变化。
附图标记说明：
1：壳体；2：第一端面；3：第二端面；4：吸附床层；5：压力检测表；
6：气流均布板；7：进气口；8：出气口；9：温度检测表；10：出液口；11：放空管；12：进气通道；13：出气通道；16：吸附剂装填入口；17：吸附剂更换排出口；18：隔板；
C1：待吸附气净化冷却装置；T1：吸附装置；K1：再生气发生装置；F1：
分离装置；
K01：水蒸汽发生器；K02：流量调节单元；K03：蒸汽锅炉软化水处理
单元；F01：冷凝器；F02：气液分离器；F03、T07：在线红外气体分析仪；F04：真空泵；F05：循环水冷却单元；T01-T04：吸附器；T05：真空设备；T06：鼓风机；T08：自控系统及仪表。
具体实施方式
为使本申请的目的、技术方案和优点更加清楚，下面将结合本申请的实施例，对本申请实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本申请一部分实施例，而不是全部的实施例。基于本申请中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本申请保护的范围。
一方面，本申请提供一种吸附器，图1为本申请一具体实施方式中的吸附器结构示意图，如图1所示，包括内部具有空腔的壳体1，以及位于空腔中的多个间隔设置的吸附床层4、多个气流均布板6，壳体1还设置有多个进气口7和出气口8，进气口7用于分别向空腔内注入待吸附气和再生气，出气口8用于输出吸附后气体和解吸气体；
相邻的两个吸附床层4之间的间隔构成通道，通道分别与进气口7和出气口8连通，且通道的宽度按照进气口、出气口的方向逐渐减少；
多个气流均布板6的入口均与进气口7连通，气流均布板的出口朝向吸附床层4；
气流均布板6的入口到气流均布板6的出口孔径逐渐减小。
本申请中的“多个”指大于等于两个，“多个”之间的数量取值可以相同也可以不同；本申请不限定各部分的具体表现形式；其中，内部具有空腔的壳体1可以为圆形或方形；
壳体1内部的空腔中设置有多个间隔分布的吸附床层4，本申请不限定吸附床层4的形状，可以为矩形、也可以为梯形，吸附床层4内部装填有吸附剂，且吸附床层4在厚度方向上设置有具有支撑作用的层，具有支撑作用的层不透过最小粒径的吸附剂且能使气体顺畅通过，可选地，具有支撑作用的层可以为织物也可以为板状结构；气流进入多个吸附床层4中进行吸附或再生处理，提高了吸附和解吸效率
气流均布板6能够实现分布和收集气流即可，气流均布板6上均匀设置有小孔，使气流均匀分布到吸附床层中，降低了床层压降，避免气流集中在某些区域，同时起到过滤待吸附气中杂质的作用，提高了吸附和解吸效率；
壳体1还设置有多个进气口7和出气口8，气体可以通过多个进气口和出气口同时进入或离开吸附器中的空腔；进气口7用于分别向空腔内注入待吸附气和再生气，出气口8用于分别输出吸附后气体和解吸气体，能够理解，当向空腔注入待吸附气时，输出的是吸附后气体；当向空腔中注入再生气时，输出的是解吸气体；
相邻的两个吸附床层4之间的间隔构成通道，通道分别与进气口7和出气口8连通，具体地，与进气口7连通的通道为进气通道12，气体通过进气通道12进入吸附床层4，与出气口8连通的通道为出气通道13，气体通过出气通道13离开吸附床层，且通道的宽度按照进气口、出气口的气流流动方向逐渐减小，由于气体通过进气口进入通道后，通道由靠近进口处到远离进口处的截面积越来越小，保持相应截面处的气流流速一致，气流能够有效利用气流均布板均布气流；
气流经进气口7进入吸附器内的空腔后，流经气流均布板6的入口，通过气流均布板的分散处理，气流得到分散均布后经气流均布板的出口离开并进入吸附床层4；气流均布板6的入口到气流均布板6的出口孔径逐渐减小，呈圆台状，可以有效均布气流，降低气流阻力以降低床层压降；
本申请提供的吸附器，通过多个吸附床层的间隔设置、多个进气口和出气口以及特殊结构的通道相互配合，使气流通过多个进气口进入吸附器内的空腔后，沿着气流流动方向依次经过气流均布板和吸附床层，可以降低床层压降，并且提高吸附和解吸效率。
可选地，多个吸附床层4在壳体1的轴向或径向方向上间隔设置；其中，至少一个进气口7设置在与通道对应的壳体上；至少一个出气口8设置在与通道对应的壳体上。
本申请不限定吸附床层4的设置方向，多个吸附床层4可以在壳体1的径向方向上间隔设置(如图1所示)，也可以在壳体1的轴向方向上间隔设置(如图2所示)；在一具体实施方式中，至少一个进气口7设置在与通道对应的壳体1上，使气流通过进气口7可以进入密闭的壳体1，待吸附气和再生气可以共用一个进气口，也可以再细分出两个并联的进气口；在另一具体实施方式中，至少一个出气口8设置在与通道对应的壳体1上，使气流通过出气口8可以离开密闭的壳体1，吸附后气体和解吸气体可以共用一个出气口，也可以再细分成两个并联的出气口。
进一步地，与进气口7对应的通道和与出气口8对应的通道不同。
能够理解，与进气口7对应的通道和与出气口8对应的通道不同，意味着每个通道能且仅能设置进气口或设置出气口，使气流进入到离开吸附器的通路上至少穿过一个吸附床层，提高吸附和解吸效率。
在一具体实施方式中，与进气口对应的通道中间设置有隔板18；
能够理解，在进气通道中间添加隔板18，能够使待吸附气进入进气通道时被平均分成两部分，有助于进一步地均布气流，减低床层压降并且提高吸附和再生效率。
具体地，吸附床层4的厚度为1-20cm。
吸附床层的厚度是指气流穿过吸附床层时的平均路径长度；能够理解，吸附床层的厚度与气流穿透其受到的阻力密切相关，申请人发现，当吸附床层4的厚度为1-20cm时，可以保证吸附和解吸效率的同时进一步降低床层压降，提高传质效率。
在本申请的一具体实施方式中，气流均布板的厚度为2-5mm；气流均布板的出口处孔径与气流均布板入口处孔径之比为1：(2-5)；
能够理解，气流均布板是具有一定厚度的分布有小孔的板状结构，由于其入口到出口的孔径逐渐减小，呈圆台状，申请人经过研究发现，当气流均布板的厚度为2-5mm，气流均布板的出口处孔径与气流均布板入口处孔径之比为1：(2-5)时，能够进一步地降低气流阻力，实现对气流的均布作用，进一步地降低床层压降；
进一步地，通道的宽度与吸附床层4的厚度比为1：(2-10)。
由于通道是沿气流的流动方向逐渐变宽的，因此通道的宽度是指平均宽度，申请人发现，当通道的宽度与吸附床层的厚度比为1：(2-10)，更有利于气流高效穿过吸附床层，降低床层压降，提高传质效率。
在一具体实施方式中，还设置有压力监测表5，压力检测表5用于监测吸附床层4在厚度方向上相对设置的第一端面2和第二端面3的压力；
本申请不限定压力检测表5的具体设置方式，可以设置在壳体1上，也可以不设置与壳体1上，凡是能够实现监测并输出吸附床层4在厚度方向上相对设置的第一端面2和第二端面3的压力即可。
另一具体实施方式中，还设置有温度监测表9，温度检测表9用于监测吸附床层4在厚度方向上相对设置的第一端面2和第二端面3的温度；
本申请不限定温度监测表9的具体设置方式，可以设置在壳体1上，也可以不设置与壳体1上，凡是能够实现监测并输出吸附床层4在厚度方向上相对设置的第一端面2和第二端面3的温度即可。
再一具体实施方式中，壳体1还设置有出液口10，出液口用于排出吸附床层4中的冷凝液；
能够理解，在吸附或解吸过程中，可能会有冷凝液产生，因此在壳体1上设置出液口10，可以排出吸附床层4和壳体1内部的冷凝液，进一步地提高传质效率，降低床层压降。
进一步地，壳体1外侧还包覆设置保温层；通过在壳体1外侧设置保温层，有利于保持吸附器内部的温度恒定，进一步的提高吸附和解吸效率，维持反应稳定性。
可选地，壳体1上还设置有吸附剂装填入口16和吸附剂更换排出口17，吸附剂填料先经吸附剂装填入口16自然装填入吸附床层4的上部，然后再使用加压空气进行辅助填充；当需要更换吸附剂时，吸附剂填料经吸附剂更换排出口17排出更换；壳体1上部还设置有放空管11，有助于调节吸附器内部的压力等等。
另一方面，本申请还提供一种上述吸附器的吸附方法，包括以下步骤：
(1)将待吸附气通过进气口送至吸附器中的空腔，通过气流均布板的分散处理后，进入吸附床层进行吸附处理，得到吸附后气体和饱和吸附床层，吸附后气体经出气口采出；
(2)对吸附器内剩余气体进行抽真空处理，直到吸附器内压力为-85kPa～-95kPa；
(3)将再生气通过进气口送至吸附器中的空腔，通过气流均布板的分散处理后，对饱和吸附床层进行再生处理，得到解吸气体、冷凝液和再生吸附床层；解吸气体经出气口采出；
(4)对再生吸附床层进行冷却处理。
本申请提供的吸附方法适用于任何直接利用固体吸附剂吸附气体的处理；具体地，步骤(1)中，将待吸附气通过进气口送至吸附器中的空腔，通过气流均布板的分散处理后，进入吸附床层进行吸附处理，去除待吸附气中的待吸附组分；能够理解，吸附器的进气口和出气口处还分别设置有气体分析仪，用于检测待气体中的待吸附组分浓度，分别得到进口浓度和出口浓度，当出口浓度与进口浓度相当时，证明吸附床层中的吸附剂吸附饱和，此时停止吸附处理，得到分离出待吸附组分后的吸附后气体和饱和吸附床层，吸附后气体通过出气口采出，离开吸附器；
步骤(2)中，对吸附器内剩余气体进行抽真空处理，直到吸附器内压力为-85kPa～-95kPa；有利于提高再生效率，降低成本；
步骤(3)中，将再生气通过进气口送至吸附器中的空腔，通过气流均布板的分散处理后，对饱和吸附床层进行再生处理，将饱和吸附床层中富集的待吸附组分解吸出来；能够理解，吸附器的出气口还连接有分离装置、气体分析仪等，用于分离并检测解吸气体的流量，当检测到解吸气体的流量为0L/min，说明吸附床层中吸附的待吸附组分已经全部解吸完成，此时停止再生处理，得到富含待吸附组分的解吸气体、冷凝液和再生吸附床层，解吸气体经出气口采出，离开吸附器，冷凝液通过出液口排出；
步骤(4)中，对再生吸附床层进行冷却处理，有利于提高下一次的吸附处理效率；步骤(1)到步骤(4)为本申请提供的吸附方法的一个循环，步骤(4)后直接进行步骤(1)即开始下一轮吸附处理。
本申请提供的上述吸附器的吸附方法，简单易行，有利于降低床层压降，提高气体的传质效率，吸附床层可无限再生，处理过程不消耗辅料，提高吸附和再生效率，有利于降低运行成本。
具体地，当待吸附气为空气、解吸气体为二氧化碳时，吸附床层包括吸附剂，吸附剂的质量与二氧化碳的吸附量之比为0.9-2mmol/g；吸附剂的粒径分布为0.3mm～1.5mm，吸附剂包括固态胺吸附材料；步骤(1)中，待吸附气的通入量为200-300Nm3/h；吸附处理的温度为20-40℃、时间为100-120min；步骤(3)中，再生气为水蒸汽，再生处理的温度为80-120℃、时间为10-30min；再生处理包括蒸汽直接吹扫再生处理。
下面以在空气中直接捕集二氧化碳为例，此时待吸附气为空气、待吸附组分和解吸气体为二氧化碳；申请人发现，吸附剂的质量与二氧化碳的吸附量之比为0.9-2mmol/g；吸附剂的粒径分布为0.3mm～1.5mm，吸附剂包括固态胺吸附材料，具体地，吸附剂为胺功能化嫁接氨基官能团的固态胺吸附材料；步骤(1)中，待吸附气的通入量为200-300Nm3/h；吸附处理的温度为20-40℃、时间为100-120min；步骤(3)中，再生气为水蒸汽，再生处理的温度为80-120℃、时间为10-30min；再生处理包括蒸汽直接吹扫再生处理；在上述参数的限定下，有利于进一步提高吸附器对空气中二氧化碳的捕集效率。
再一方面，本申请还提供一种吸附系统，包括上述的吸附器。
通过包括上述吸附器的吸附系统，能够降低气体在吸附器中的床层压降，提高吸附和再生效率，降低运行成本。
具体地，图3为本申请一具体实施方式中的吸附系统示意图，如图3所示，还包括待吸附气净化冷却装置C1、吸附装置T1、再生气发生装置K1、分离装置F1；
其中，吸附装置T1包括至少一个吸附器；
待吸附气净化冷却装置C1的出口与吸附器的进气口连通，吸附器的出气口用于输出吸附后气体；
再生气发生装置K1的出口与吸附器的进气口连通，吸附器的出气口还与分离装置F1的入口连通，分离装置F1的气相出口用于输出产品气，分离装置F1的液相出口与再生气发生装置K1的回流口连通。
在本申请的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“连通”、“连接”应作广义理解，例如，可以使固定连接，也可以是通过中介媒介间相连，可以是两个元件内部的连通或者两个元件的相互作用关系。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本申请中的具体含义；
本申请不限定各个单元的具体表现形式，其中，待吸附气净化冷却装置C1能够实现过滤待吸附气中的杂质并且使其降温即可；吸附装置T1包括至少一个上述吸附器，各个吸附器间可以采用并联或串连；再生气发生装置K1能够产生再生气即可；分离装置F1能够实现将解吸气体中的待吸附组分与再生气分离即可；
具体地，待吸附气净化冷却装置C1的入口即为吸附系统的入口，待吸附气通过待吸附气净化冷却装置C1的入口进入待吸附气净化冷却装置C1，在其中进行过滤净化并降温，通过待吸附气净化冷却装置C1的出口离开，并通过吸附器的进气口进入吸附装置T1内，在其中进行吸附处理，吸附处理结束后，得到吸附后气体和饱和吸附床层；吸附后气体通过吸附器的出气口采出，离开吸附系统；再生气发生装置K1的出口也与吸附器的进气口连通，再生气通过再生气发生装置K1的出口产出后通过吸附器的进气口进入吸附器，对饱和吸附床层进行再生处理，将饱和吸附床层中的待吸附组分解吸出来，得到再生吸附床层和解吸气体，解吸气体通过吸附器的出气口采出，通过分离装置F1的入口进入分离装置F1，在其中待吸附组分与再生气分离，得到解吸气体和再生循环液，解吸气体通过分离装置F1的气相出口离开，输出产品气，再生循环液与再生气发生装置K1的回流口连通，回收再生气。
图4为本申请一具体实施方式中的吸附系统示意图，如图4所示，当吸附系统用于在空气中直接捕集二氧化碳时，再生气发生装置包括水蒸汽发生器K01和流量调节单元K02等；其中，水蒸汽发生器K01用以将常温供给水加热至沸腾并产生足量水蒸汽用以加热吸附剂；流量调节单元K02主要包括开度调节阀门以及流量计，通过PID控制系统进行蒸汽的流量调节；
分离装置包括冷凝器F01、气液分离器F02、在线红外气体分析仪F03、真空泵F04、循环水冷却单元F05等；其中，冷凝器F01用于将脱附后的二氧化碳和水蒸汽的混合气冷凝到一定温度，并去除掉其中的大部分水；气液分离器F02用于将二氧化碳气体与水的分离；在线红外气体分析仪F03用于检测分离得到的二氧化碳产品气的纯度；真空泵F04有助于将气液分离出的二氧化碳产品气抽出；循环水冷却单元F05用于对冷凝器F01进行循环冷却降温；
吸附装置中包括四个并联的吸附器T01-T04、真空设备T05、鼓风机T06、在线红外气体分析仪T07、自控系统及仪表T08等等；其中，真空设备T05用于抽取吸附器中剩余的空气，并在解吸和再生气过程中及时抽出残余气体，加快吸附和再生效率；鼓风机T06用于将空气通入吸附器内并能克服足够的沿程阻力；在线红外气体分析仪T07用于实时检测吸附器的进气口和出气口的浓度变化；自控系统及仪表T08用于及时进行流量调节，其中所有阀门均与可编程逻辑控制器(PLC)连接，由PLC控制器控制整个系统的运行；
可选地，吸附系统还包括蒸汽锅炉软化水处理单元K03，用于处理吸附塔底部冷凝段的排出液体；具体地，吸附器的出液口、气液分离器的液相出口分别与蒸汽锅炉软化水处理单元的入口连通，蒸汽锅炉软化水处理单元的出口与水蒸汽发生器的回流口连通。
以下，通过具体实施例对本申请提供的吸附器进行详细的介绍。
实施例1
本实施例采用如图1所示的吸附器，其中，4个吸附床层在轴向上间隔设置，进气口数量为2个、出气口数量为3个和均布板数量为4个；吸附床层的厚度为10cm；通道的宽度与吸附床层的厚度比为1:2；气流均布板的厚度为3mm；气流均布板的出口处孔径与气流均布板入口处孔径之比为1：3；
本实施例对空气中的二氧化碳进行吸附处理，空气中的二氧化碳浓度为400ppm，包括以下步骤：
(1)将空气通过进气口送至吸附器中的空腔，空气的通入量为260Nm3/h，通过气流均布板的分散处理后，进入吸附床层进行吸附处理，吸附床层中设置的吸附剂为胺功能化嫁接氨基官能团的固态胺吸附材料，其粒径为0.6mm；吸附处理的温度为20℃、时间为120min，得到吸附后空气和饱和吸附床层，吸附后空气经出气口采出；
(2)对吸附器内剩余气体进行抽真空处理，抽真空处理的时间为5min，吸附器内压力为-95kPakPa；
(3)将水蒸汽通过进气口送至吸附器中的空腔，水蒸汽的通入量为1Nm3/h，通过气流均布板的分散处理后，对饱和吸附床层进行再生处理，再生处理采用蒸汽直接吹扫，再生处理的温度为120℃、时间为15min，得到二氧化碳、冷凝液和再生吸附床层；二氧化碳经出气口采出；
(4)通入空气对再生吸附床层进行冷却处理，冷却处理的温度为环境温度、时间为10min。
实施例2
本实施例与实施例1的区别在于：步骤(1)中，吸附处理时间为60min。
实施例3
本实施例与实施例1的区别在于，步骤(1)中，吸附处理时间为180min。
实施例4
本实施例与实施例1的区别在于：步骤(1)中，吸附处理温度为10℃。
实施例5
本实施例与实施例1的区别在于：步骤(3)中，再生处理采用水蒸汽辅助换热。
实施例6
本实施例与实施例1的区别在于：采用如图2所示的吸附器，其中，4个吸附床层在轴向上间隔设置，进气口数量为2个、出气口数量为2个和均布板数量为2个；吸附床层的厚度为10cm；通道的宽度与吸附床层的厚度比为1:2。
实施例7
本实施例与实施例1的区别在于：吸附床层的厚度为20cm。
实施例8
本实施例与实施例1的区别在于：通道的宽度与吸附床层的厚度比为1：10。
对比例1
本对比例与实施例1的区别在于：吸附床层数量为1个，进气口数量为1个、出气口数量为1个和均布板数量为1个；吸附床层的厚度为40cm。
试验例1
对实施例与对比例中的吸附后空气通过在线红外气体分析仪进行检测；其中，CO2平均吸附量＝(进口浓度-出口浓度)×风流流量×吸附时间/吸附剂质量；
CO2捕集率的计算公式:
其中，CCR为CO2捕集率，单位为％；为吸附时间内出气口CO2平均浓度，为吸附时间内进气口CO2平均浓度，单位为ppm；Qfeed为吸附时间内出口流量，Qpurge为吸附时间内出口流量，单位为L/min；
其中，床层压降由经典Ergun公式计算：
Z为吸附床层的厚度，单位为cm；ε为吸附床层孔隙率，单位为％；dp为吸附剂平均粒径，单位为mm；u为吸附床层表观流速，单位为m/s；ρ为气体密度，单位为kg/m3；μ为气体黏度，单位为Pa·s。
测得结果如图5、6以及表1所示。
图5为吸附出口CO2浓度随吸附时间变化图，其中，图例1、3-6为吸附时间60min的重复试验，图例2为吸附时间为180min，图例7-10为吸附时间120min的重复试验；图6为吸附出口CO2吸附量随吸附时间变化图；由图可知，当吸附时间为60min时，吸附量为0.88～1.1mmol/g；当吸附时间为120min时，吸附量为1.35～1.62mmol/g，同时当吸附时间为180min时，吸附量仅增加13％。吸附时间为100～120min时，已占饱和吸附量的80％以上，故本申请推荐吸附时长为100～120min，在保证吸附效率的同时降低运行成本。
表1
由表1可知，相比于对比例1，本申请提供的吸附器和吸附方法能够有效降低床层压降，提高了对二氧化碳的吸附和再生效率。
试验例2
利用温度监测表测试实施例1和实施例5中再生处理中吸附床层的温度变化，结果如图7所示。
图7为不同再生处理方式的再生速率对比图，其中，辅助换热再生与直接蒸汽吹扫再生均为两次重复试验；由图7可知，实施例5中水蒸汽辅助换热的平均温度为82℃左右，再生时间较长为90min；实施例1中蒸汽直接吹扫再生的平均温度为100℃左右，再生时间为25min左右；因此使用蒸汽直接吹扫再生可大大提高再生速率，缩短再生时间，提高吸附器运行效率。
试验例3
对实施例1与实施例4中的吸附后空气通过在线红外气体分析仪进行检测，通过温度监测表对吸附处理中吸附床层的温度进行检测，得到图8。
图8为不同温度下的吸附量变化图，实施例4中吸附过程平均温度35～40℃，60min的平均吸附量在0.65mmol/g左右；实施例1中吸附过程平均温度为15～20℃，60min的平均吸附量在0.97mmol/g左右；可见较低的吸附温度有利于吸附过程的进行，因此吸附温度在10-20℃时，更有利于确保高效吸附。
试验例4
利用压力检测表检测对实施例1步骤(2)抽真空处理中吸附器内压力变化，结果如图9所示。
图9为抽真空处理中压力随时间变化图，由图可知，在5-10min内可使吸附器内压力降至目标值。
试验例5
利用温度监测表测试实施例1步骤(4)冷却处理中吸附床层的温度变化，结果如图10所示。
图10为冷却处理中温度随时间变化，使用空气降温可在10min左右将床层温度降至室温，提高了冷却效率，降低再生过程的能耗，大大减少吸附器再生冷却操作时间并缩短吸/脱附循环周期时间。
最后应说明的是：以上各实施例仅用以说明本申请的技术方案，而非对其限制；尽管参照前述各实施例对本申请进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本申请各实施例技术方案的范围。

Claims (20)

  1. 一种吸附器，其中，包括内部具有空腔的壳体，以及位于所述空腔中的多个间隔设置的吸附床层、多个气流均布板，所述壳体还设置有多个进气口和出气口，所述进气口用于分别向所述空腔内注入待吸附气和再生气，所述出气口用于输出吸附后气体和解吸气体；
    相邻的两个所述吸附床层之间的间隔构成通道，所述通道分别与所述进气口和出气口连通，且所述通道的宽度按照进气口、出气口的方向逐渐减小；
    多个所述气流均布板的入口均与所述进气口连通，所述气流均布板的出口朝向所述吸附床层；
    所述气流均布板的入口到所述气流均布板的出口孔径逐渐减小。
  2. 根据权利要求1所述的吸附器，其中，多个所述吸附床层在所述壳体的轴向或径向方向上间隔设置；其中，至少一个所述进气口设置在与所述通道对应的壳体上。
  3. 根据权利要求2所述的吸附器，其中，至少一个所述出气口设置在与所述通道对应的壳体上。
  4. 根据权利要求3所述的吸附器，其中，与所述进气口对应的通道和与所述出气口对应的通道不同。
  5. 根据权利要求2-4任一项所述的吸附器，其中，与所述进气口对应的通道中间设置有隔板。
  6. 根据权利要求1-5任一项所述的吸附器，其中，所述吸附床层的厚度为1-20cm。
  7. 根据权利要求1-6任一项所述的吸附器，其中，所述气流均布板的厚度为2-5mm。
  8. 根据权利要求1-7任一项所述的吸附器，其中，所述气流均布板的出口处孔径与所述气流均布板入口处孔径之比为1：(2-5)。
  9. 根据权利要求1-8任一项所述的吸附器，其中，所述通道的宽度与所述吸附床层的厚度比为1：(2-10)。
  10. 根据权利要求1-9任一项所述的吸附器，其中，还设置有压力监测表，所述压力检测表用于监测所述吸附床层在厚度方向上相对设置的第一端面和第二端面的压力。
  11. 根据权利要求1-10任一项所述的吸附器，其中，还设置有温度监测表，所述温度检测表用于监测所述吸附床层在厚度方向上相对设置的第一端面和第二端面的温度。
  12. 根据权利要求1-11任一项所述的吸附器，其中，壳体还设置有出液口，所述出液口用于排出所述吸附床层中的冷凝液。
  13. 根据权利要求1-11任一项所述的吸附器，其中，所述壳体外侧还包覆设置保温层。
  14. 一种权利要求1-13任一项所述的吸附器的吸附方法，其中，包括以下步骤：
    (1)将待吸附气通过进气口送至所述吸附器中的空腔，通过气流均布板的分散处理后，进入吸附床层进行吸附处理，得到吸附后气体和饱和吸附床层，所述吸附后气体经出气口采出；
    (2)对所述吸附器内剩余气体进行抽真空处理，直到所述吸附器内压力为-85kPa～-95kPa；
    (3)将再生气通过所述进气口送至所述吸附器中的空腔，通过所述气流均布板的分散处理后，对所述饱和吸附床层进行再生处理，得到解吸气体、冷凝液和再生吸附床层；所述解吸气体经所述出气口采出；
    (4)对所述再生吸附床层进行冷却处理。
  15. 根据权利要求14所述的吸附方法，其中，当所述待吸附气为空气、所述解吸气体为二氧化碳时，所述吸附床层包括吸附剂，所述吸附剂的质量与所述二氧化碳的吸附量之比为0.9-2mmol/g。
  16. 根据权利要求14或15所述的吸附方法，其中，所述吸附剂的粒径分布为0.3mm～1.5mm，所述吸附剂包括固态胺吸附材料。
  17. 根据权利要求14-16任一项所述的吸附方法，其中，步骤(1)中，所述待吸附气的通入量为200-300Nm3/h；所述吸附处理的温度为20-40℃、时间为100-120min。
  18. 根据权利要求14-17任一项所述的吸附方法，其中，步骤(3)中，所述再生气为水蒸汽，所述再生处理的温度为80-120℃、时间为10-30min；所述再生处理包括蒸汽直接吹扫再生处理。
  19. 一种吸附系统，其中，包括权利要求1-13任一项所述的吸附器。
  20. 根据权利要求19所述的吸附系统，其中，还包括待吸附气净化冷却装置、吸附装置、再生气发生装置、分离装置；
    其中，所述吸附装置包括至少一个所述吸附器；
    所述待吸附气净化冷却装置的出口与所述吸附器的进气口连通，所述吸附器的出气口用于输出吸附后气体；
    所述再生气发生装置的出口与所述吸附器的进气口连通，所述吸附器的出气口还与所述分离装置的入口连通，所述分离装置的气相出口用于输出产品气，所述分离装置的液相出口与所述再生气发生装置的回流口连通。
PCT/CN2024/136128 2024-03-25 2024-12-02 一种吸附器、吸附系统及吸附方法 Pending WO2025200538A1 (zh)

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