Waste gas treatment method, device and application

Abstract

The invention relates to the technical field of environmental protection, and discloses a waste gas treatment method and device and application. The method is carried out in a waste gas treatment device, the waste gas treatment device comprises a packed tower, and the packed tower comprises a packing absorption section, an atomization spraying section and a packing desorption section which are sequentially arranged from top to bottom. According to the method and the device, the non-methane waste gas with the total VOCs concentration not larger than 1500 g / m < 3 > is treated, the liquefaction recovery efficiency of light hydrocarbon is high, the VOCs content in purified gas is not higher than 60 mg / m < 3 >, safety and environmental protection are achieved, hazardous waste is not generated, the treatment cost is low, and economic benefits are high.

Description

Technical Field

[0001] The present invention relates to the field of environmental protection, and particularly to a method, device and application for waste gas treatment. Background Art

[0002] Currently, the treatment of non-methane hydrocarbon VOCs usually adopts the method of adsorption beds. However, during the vacuum regeneration process of this method, the highest concentration of the enriched gas is only 70 vol% - 80 vol%, the enrichment efficiency of light hydrocarbons is low, the liquefaction and condensation are difficult, and the content of VOCs in the discharged clean gas is high.

[0003] In order to meet the emission standards, it is usually necessary to use an adsorbent for auxiliary absorption. However, the service life of the adsorbent is short, and the desorption is not complete, so it needs to be replaced frequently. The replacement of the waste adsorbent also belongs to a kind of hazardous waste, which is highly unfriendly to the environment. Summary of the Invention

[0004] The first object of the present invention is to treat non-methane VOCs waste gas so that the content of VOCs in the clean gas discharged from the packed tower does not exceed 60 mg / m 3 ;

[0005] The second object of the present invention is to improve the enrichment rate of VOCs and recover liquid light hydrocarbons while achieving the first object.

[0006] To achieve the above objects, the first aspect of the present invention provides a method for waste gas treatment, which is carried out in a waste gas treatment device. The waste gas treatment device includes a packed tower, and the packed tower includes a packing absorption section, an atomizing spray section and a packing desorption section arranged in sequence from top to bottom;

[0007] The method includes:

[0008] S1: Introduce the waste gas into the atomizing spray section for the first contact treatment with the absorbent droplets to obtain rich liquid and lean gas;

[0009] S2: Introduce the lean gas into the packing absorption section for the second contact treatment with the absorbent to obtain clean gas and lean liquid; and,

[0010] Introduce the rich liquid into the packing desorption section for desorption treatment to obtain rich gas and a circulating absorbent for recycling to the packing absorption section and / or the atomizing spray section;

[0011] Wherein, in step S1, the concentration of non-methane total VOCs in the waste gas is not greater than 1500 g / m 3 ; the absorbent droplets are obtained by atomizing the absorbent and / or the lean liquid, and the average particle diameter of the absorbent droplets is not greater than 1000 μm;

[0012] Among them, the inlet volume flow rate of the waste gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent contacting the lean gas = Q: 0.005Q - 0.02Q: 0.005Q - 0.02Q. The second aspect of the present invention provides a waste gas treatment device, which includes a packed tower. The packed tower includes a packed absorption section, an atomizing spray section, and a packed desorption section arranged in sequence from top to bottom. A clean gas discharge port is provided at the top of the packed tower;

[0013] The atomizing spray section includes an atomizing spray unit and a rich liquid accommodation area arranged below the atomizing spray unit. The atomizing range of the atomizing spray unit is not greater than 1000 μm, and a waste gas inlet is also provided between the atomizing spray unit and the rich liquid accommodation area;

[0014] The packed absorption section includes a liquid distributor I and a packed absorption area arranged between the liquid distributor I and the atomizing spray unit;

[0015] The packed desorption section includes a liquid distributor II, a packed desorption area, and a recycled absorbent regeneration area arranged in sequence from top to bottom. The liquid distributor II is arranged below the rich liquid accommodation area.

[0016] The third aspect of the present invention provides the application of the aforementioned method and / or the aforementioned device in waste gas treatment.

[0017] The waste gas treatment method provided by the present invention treats waste gas with a non-methane total VOCs concentration of not greater than 1500 g / m 3 The liquefaction recovery efficiency of light hydrocarbons is high, the VOCs content in the clean gas is not higher than 60 mg / m 3 , it is safe and environmentally friendly without generating hazardous waste, the treatment cost is low, and the economic benefit is high.

[0018] The waste gas treatment device provided by the present invention has a simple structure, low investment cost, high efficiency in treating waste gas with a non-methane total VOCs concentration of not greater than 1500 g / m 3 , it is environmentally friendly and safe, and the device operates stably. Description of the Drawings

[0019] Figure 1 is a structural schematic diagram of a waste gas treatment device provided by some preferred embodiments of the present invention;

[0020] Figure 2 is a structural schematic diagram of a waste gas treatment device provided by other preferred embodiments of the present invention.

[0021] Description of the Reference Numerals

[0022] 1. Exhaust gas inlet pipeline; 2. Inlet fan; 3. Atomizing nozzle; 4. Packed absorption zone; 5. Liquid distributor I; 6. Demister II; 7. Clean gas discharge pipeline; 8. Automatic control valve II; 9. Automatic control valve III; 10. Atomizing spray unit; 11. Rich liquid holding zone; 12. Automatic control valve I; 13. Liquid level monitor I; 14. Liquid distributor II; 15. Packed desorption zone; 16. Circulating absorbent regeneration zone; 17. Circulation pump; 18. Demister I; 19. Vacuum pump; 20. Condensation unit; 21. Delivery pump; 22. Control valve I; 23. Control valve II; 24. Liquid level monitor II; 25. Compressor. Detailed implementation manners

[0023] In order to make the technical problems, technical solutions and beneficial effects to be solved by the present invention more clearly understood, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0024] It should be noted that when an element is referred to as being "fixed to" or "disposed on" another element, it can be directly on the other element or indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or indirectly connected to the other element.

[0025] It should be understood that the orientation or positional relationship indicated by the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. is based on the orientation or positional relationship shown in the accompanying drawings, and is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention.

[0026] In the ranges disclosed herein, the endpoints and any values are not limited to the exact ranges or values, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, between the endpoint values of each range, between the endpoint values of each range and individual point values, and between individual point values, they can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be regarded as specifically disclosed herein.

[0027] As described above, the first aspect of the present invention discloses a method for treating exhaust gas, which is carried out in an exhaust gas treatment device. The exhaust gas treatment device includes a packed tower, and the packed tower includes a packed absorption section, an atomizing spray section and a packed desorption section which are arranged in sequence from top to bottom;

[0028] The method includes:

[0029] S1: Introduce the waste gas into the atomizing spray section for the first contact treatment with the absorbent droplets to obtain rich liquid and lean gas;

[0030] S2: Introduce the lean gas into the packed absorption section for the second contact treatment with the absorbent to obtain clean gas and lean liquid; and,

[0031] Introduce the rich liquid into the packed desorption section for desorption treatment to obtain rich gas and a circulating absorbent for recycling to the packed absorption section and / or the atomizing spray section;

[0032] Wherein, in step S1, the concentration of total non-methane VOCs in the waste gas is not more than 1500 g / m 3 ; the absorbent droplets are obtained by atomizing the absorbent and / or the lean liquid, and the average particle diameter of the absorbent droplets is not more than 1000 μm;

[0033] Wherein, the inlet volume flow rate of the waste gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent contacting the lean gas = Q: 0.005Q - 0.02Q: 0.005Q - 0.02Q.

[0034] The waste gas treatment method provided by the present invention treats waste gas with a total non-methane VOCs concentration of not more than 1500 g / m 3 The VOCs content in the clean gas is not higher than 60 mg / m 3 , which is safe, environmentally friendly, does not produce hazardous waste, has low treatment costs and high economic benefits.

[0035] It should be noted that the present invention does not make special limitations on the treatment method of the clean gas. Exemplarily: In some embodiments, the clean gas is directly discharged into the air.

[0036] It should also be noted that the circulating absorbent is the absorbent obtained by desorbing the rich liquid, and its composition and effect are not much different from the fresh absorbent in step 2, and the circulating absorbent can be directly used as the fresh absorbent.

[0037] According to some preferred embodiments of the present invention, the average particle diameter of the absorbent droplets is 10 μm - 1000 μm. Under this preferred condition, the effect of absorbing VOCs in the waste gas is better, and the VOCs content in the discharged clean gas is lower.

[0038] More preferably, the average particle diameter of the absorbent droplets is 10 μm - 500 μm. Under this preferred condition, the effect of absorbing VOCs in the waste gas is better, and the VOCs content in the discharged clean gas is lower.

[0039] According to some preferred embodiments of the present invention, the method further comprises the following steps:

[0040] S3: Condensing the rich gas to obtain liquid light hydrocarbons and non-condensable gas; and,

[0041] Introducing the lean liquid into the atomizing spray section for first contact treatment with the waste gas, or introducing the lean liquid into the packing desorption section for desorption treatment;

[0042] S4: Returning the non-condensable gas to the atomizing spray section for the first contact treatment.

[0043] Under this preferred condition, stable liquid light hydrocarbons can also be produced, with higher economic benefits.

[0044] According to some preferred embodiments of the present invention, based on the total mass of all non-methane VOCs in the waste gas, the content of non-aromatic hydrocarbons is not less than 10 vol%, and the temperature of the condensation treatment is 0°C to -120°C, preferably -20°C to -30°C. Under this preferred condition, the efficiency of liquefying and recovering liquid light hydrocarbons is higher, and the recovery rate of liquid light hydrocarbons is also higher.

[0045] According to some preferred embodiments of the present invention, based on the total mass of all non-methane VOCs in the waste gas, the content of non-aromatic hydrocarbons is less than 0.5 vol%, and the temperature of the condensation treatment is 3°C to 15°C. Under this preferred condition, the efficiency of liquefying and recovering liquid light hydrocarbons is higher, and the recovery rate of liquid light hydrocarbons is also higher.

[0046] According to some preferred embodiments of the present invention, in step S3, the rich gas is withdrawn from the packing desorption section and subjected to condensation treatment. More preferably, the extraction volume flow rate of the rich gas in step S3: the inlet volume flow rate of the waste gas in step S1 = 0.25Q - 0.8Q:Q. Under this preferred condition, the desorption treatment can be carried out more thoroughly, the impurity content of the recycled absorbent obtained by desorption is less, the enrichment rate of VOCs is higher, and the content of VOCs in the rich gas is higher.

[0047] According to some preferred embodiments of the present invention, in step S2, the pressure of the desorption treatment is -90 kPa to -101 kPa in gauge pressure, and the temperature is 10°C to 50°C. Under this preferred condition, the impurity content of the recycled absorbent obtained by desorption is less, the enrichment rate of VOCs is higher, and the content of VOCs in the rich gas is higher.

[0048] According to some preferred embodiments of the present invention, in step S1, the absorbent contains a composite component, a hydrogen bond donor, and a hydrogen bond acceptor. The molar ratio of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1:0.5 - 10:0.01 - 0.2. The hydrogen bond acceptor is selected from at least one of menthol, thymol, lidocaine, and quaternary ammonium salts. The hydrogen bond donor is selected from at least one of fatty acids. The composite component is a mixture of component A and component B. Component A is selected from at least one of p-xylene, methylcyclohexane, dipentene, terpinene, toluene, and n-hexane. Component B is selected from at least one of citronellol, 4-8 saturated monohydric aliphatic alcohols of C

[0049] It should be noted that in the present invention, the 4-8 saturated monohydric aliphatic alcohols of C include saturated monohydric aliphatic alcohols of C4, C5, C6, C7, and C8.

[0050] It should be noted that in the present invention, the saturated vapor pressure of the absorbent is measured by thermogravimetric analysis, and the saturated water content is measured according to the Karl Fischer titration method.

[0051] More preferably, in the composite component, the molar ratio of component A to component B is 1:0.1 - 1. Under this preferred condition, the absorbent has a better effect on absorbing VOCs. The content of VOCs in the clean gas discharged from the treated waste gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0052] According to some preferred embodiments of the present invention, based on the total mass of all non-methane VOCs in the waste gas, when the content of alkanes is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents:

[0053] The molar ratio of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1:1 - 4:0.01 - 0.1;

[0054] The hydrogen bond acceptor is selected from at least one of the menthol, thymol, and lidocaine;

[0055] The hydrogen bond donor is selected from at least one of saturated fatty acids of C 12-18 and monounsaturated fatty acids of C 12-18 ;

[0056] The component A is at least one of the p-xylene and the methylcyclohexane, and the component B is at least one of the citronellol and the saturated monohydric fatty alcohol of C 4-8 Under this preferred condition, the content of VOCs in the clean gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0057] It should be noted that in the present invention, the saturated fatty acid of C 12-18 includes saturated fatty acids of C 12 saturated fatty acids of C 13 saturated fatty acids of C 14 saturated fatty acids of C 15 saturated fatty acids of C 16 saturated fatty acids of C 17 saturated fatty acids of C 18 Similarly, the monounsaturated fatty acids of C 12-18 include monounsaturated fatty acids of C 12 monounsaturated fatty acids of C 13 monounsaturated fatty acids of C 14 monounsaturated fatty acids of C 15 monounsaturated fatty acids of C 16 monounsaturated fatty acids of C 17 monounsaturated fatty acids of C 18 monounsaturated fatty acids of C.

[0058] According to some preferred embodiments of the present invention, based on the total mass of all non-methane VOCs in the waste gas, when the content of olefins is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents:

[0059] The molar ratio of the contents of the hydrogen bond acceptor, the hydrogen bond donor, and the composite component is 1:1-8:0.01-0.2;

[0060] The hydrogen bond acceptor is selected from at least one of the menthol and the quaternary ammonium bromide;

[0061] The hydrogen bond donor is selected from at least one of the fatty acids with the molecular formula R 1 -COOH, and R 1 is selected from an alkyl group of C6-C 10 and an alkenyl group of C 16 -C 18 ;

[0062] The component A is selected from at least one of the dipentene and the terpinene, and the component B is selected from at least one of the ethyl benzoate and the isophorone. Under this preferred condition, the content of VOCs in the clean gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0063] According to some preferred embodiments of the present invention, based on the total mass of all non-methane VOCs in the waste gas, when the content of aromatic hydrocarbons is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents:

[0064] The molar ratio of the contents of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1:0.5 - 10:0.02 - 0.2;

[0065] The hydrogen bond acceptor is selected from at least one of the quaternary ammonium salt, menthol, and thymol, and the structure of the quaternary ammonium salt is Each R 2 is selected from one of the alkyl groups of C 4-8 and L is Cl or Br;

[0066] The hydrogen bond donor is selected from at least one of the fatty acids with the molecular formula R 3 -COOH, wherein R 3 is C n H 2n+1 or C n H 2n-1 , n is an integer from 5 to 17, and exemplarily, n is any one of 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17;

[0067] Component A is selected from at least one of toluene and n-hexane, and component B is selected from at least one of acetic acid, lactic acid, and pyruvic acid. Under this preferred condition, the content of VOCs in the clean gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0068] According to some preferred embodiments of the present invention, in step S1, the temperature of the absorbent droplets is 10°C - 50°C. Under this preferred condition, the content of VOCs in the clean gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0069] According to some preferred embodiments of the present invention, in step S2, the temperature of the absorbent is 10°C - 50°C. Under this preferred condition, the content of VOCs in the clean gas is lower, the content of VOCs in the rich gas is higher, and the enrichment rate of VOCs is higher.

[0070] According to some preferred embodiments of the present invention, in step S2, the packing filled in the packing absorption section is at least one of perforated plate corrugated packing, plate corrugated packing, wire mesh corrugated packing, Raschig ring, Pall ring, and theta ring.

[0071] According to some preferred embodiments of the present invention, in step S2, the packing in the packing desorption section is at least one of orifice corrugated packing, plate corrugated packing, wire mesh corrugated packing, Raschig ring, Pall ring, and theta ring.

[0072] According to some preferred embodiments of the present invention, a clean gas discharge port is provided at the top of the packed tower;

[0073] The atomizing spray section includes an atomizing spray unit 10 and a rich liquid receiving area 11 provided below the atomizing spray unit 10. The atomizing range of the atomizing spray unit 10 is not greater than 1000 μm, and an exhaust gas inlet is further provided between the atomizing spray unit 10 and the rich liquid receiving area 11;

[0074] The packing absorption section includes a liquid distributor I5 and a packing absorption area 4 provided between the liquid distributor I5 and the atomizing spray unit 10;

[0075] The packing desorption section includes a liquid distributor II14, a packing desorption area 15, and a circulating absorbent regeneration area 16 arranged in sequence from top to bottom. The liquid distributor II14 is provided below the rich liquid receiving area 11.

[0076] It should be noted that the atomizing range of the atomizing spray unit 10 being not greater than 1000 μm means that the atomizing spray unit 10 can atomize the absorbent into absorbent droplets with an average particle diameter of not greater than 1000 μm.

[0077] According to some preferred embodiments of the present invention, the exhaust gas treatment device further includes a condensation unit 20. A rich gas extraction port communicated with the condensation unit 20 is further provided between the liquid distributor II14 and the rich liquid receiving area 11, and the condensation unit 20 is also communicated with the exhaust gas inlet.

[0078] According to some preferred embodiments of the present invention, the circulating absorbent regeneration area 16 is also independently communicated with the atomizing spray unit 10 and the liquid distributor I5 through a circulating pump 17.

[0079] The present invention provides a preferred step flow of an exhaust gas treatment method, including:

[0080] S1: Introduce the exhaust gas directly into the atomizing spray unit 10 and the rich liquid receiving area 11, and perform a first contact treatment with the absorbent droplets sprayed by the atomizing spray unit 10 to obtain lean gas that continues to rise and rich liquid that falls into the rich liquid receiving area 11;

[0081] S2: The lean gas rises to the packing absorption area 4 and performs a second contact treatment with the absorbent sprinkled by the liquid distributor I5 to obtain clean gas and lean liquid, and the clean gas is discharged from the clean gas discharge port; and,

[0082] Introduce the rich liquid from the rich liquid accommodation area 11 into the liquid distributor II 14, and the liquid distributor II 14 distributes the rich liquid in the packing desorption area 15 for desorption treatment to obtain rich gas and recycled absorbent;

[0083] It should be noted that the lean liquid continues to fall to the atomization spraying section to make the first contact treatment with the waste gas, generating rich liquid and lean gas again, or, directly introduce the lean liquid into the liquid distributor II 14, and the liquid distributor II 14 distributes the lean liquid in the packing desorption area 15 for desorption treatment to obtain rich gas and recycled absorbent;

[0084] S3: Extract the rich gas from the packing desorption section and transport it to the condensation unit 20 for condensation treatment to obtain liquid light hydrocarbons and non-condensable gas; and

[0085] Introduce the recycled absorbent into the atomization spraying unit 10 and / or the liquid distributor I 5 through the recycle pump 17.

[0086] The second aspect of the present invention provides an exhaust gas treatment device, as Figure 1 and Figure 2 shown, the exhaust gas treatment device includes a packed tower, and the packed tower includes a packing absorption section, an atomization spraying section and a packing desorption section which are arranged in sequence from top to bottom. A clean gas discharge port is provided at the top of the packed tower;

[0087] The atomization spraying section includes an atomization spraying unit 10 and a rich liquid accommodation area 11 arranged below the atomization spraying unit 10. An exhaust gas inlet is also provided between the atomization spraying unit 10 and the rich liquid accommodation area 11;

[0088] The packing absorption section includes a liquid distributor I 5 and a packing absorption area 4 arranged between the liquid distributor I 5 and the atomization spraying unit 10;

[0089] The packing desorption section includes a liquid distributor II 14, a packing desorption area 15 and a recycled absorbent regeneration area 16 which are arranged in sequence from top to bottom. The liquid distributor II 14 is arranged below the rich liquid accommodation area 11.

[0090] The VOCs exhaust gas treatment device provided by the present invention is provided with two VOCs absorption areas, namely an atomization spraying section and a packing absorption section. In practical applications, the VOCs exhaust gas is first subjected to atomization spraying absorption treatment and packing absorption treatment, and then the rich liquid is subjected to packing desorption treatment. The content of VOCs in the obtained rich gas can reach more than 90 vol%, and the content of VOCs in the clean gas discharged from the clean gas discharge port at the top of the packed tower is not higher than 60 mg / kg.

[0091] As Figure 1 shown, the present invention provides a preferred application process of the VOCs exhaust gas treatment device, and this process includes the following steps:

[0092] S1: Introduce the VOCs waste gas into the atomizing spray section for first contact treatment with the absorbent droplets sprayed by the atomizing spray unit 10 to obtain rich liquid and lean gas; the rich liquid is stored in the rich liquid accommodation area 11;

[0093] S2: The lean gas rises to the packing absorption area 4 for second contact treatment with the absorbent liquid material sprayed by the liquid distributor I 5 to obtain clean gas and lean absorbent; and,

[0094] Introduce the rich liquid into the packing desorption section and spray it onto the packing desorption area 15 through the liquid distributor II 14. After desorption treatment, rich gas and recycled absorbent for recycling to the packing absorption section and / or the atomizing spray section are obtained.

[0095] It should be noted that in the present invention, there is no special limitation on the treatment method of the clean gas. Exemplarily: in some embodiments, the clean gas is directly discharged into the air.

[0096] In other embodiments, the VOCs waste gas treatment device further includes a clean gas discharge pipeline 7 connected to the clean gas discharge port, and the clean gas is transported to a clean gas storage tank for storage or used for other purposes through the clean gas discharge pipeline 7 according to actual needs.

[0097] According to some preferred embodiments of the present invention, the atomizing range of the atomizing spray unit 10 is not greater than 1000 μm. Under this preferred condition, the absorption efficiency of the absorbent for VOCs can be further improved, and the content of VOCs in the enriched rich gas can reach 97%.

[0098] According to a further preferred embodiment of the present invention, the atomizing spray unit 10 includes at least 1 atomizing nozzle 3. The atomizing nozzle 3 is provided with a plurality of spray holes, the aperture of the spray holes is 10 μm - 100 μm, the number of the spray holes is set to 1 - 100, preferably 10 - 40, and the spray holes are arranged in a square array, a circular array or a circular arrangement.

[0099] According to some preferred embodiments of the present invention, a condensation unit 20 is further included. A rich gas extraction port communicating with the condensation unit 20 is further provided between the liquid distributor II 14 and the rich liquid accommodation area 11, and the condensation unit 20 is also communicated with the waste gas inlet.

[0100] As Figure 1 shown, the present invention provides another preferred application process of the VOCs waste gas treatment device, and this process includes the following steps:

[0101] S1: Introduce the VOCs waste gas into the atomizing spray section for first contact treatment with the absorbent droplets sprayed by the atomizing spray unit 10 to obtain rich liquid and lean gas; the rich liquid is stored in the rich liquid accommodation area 11;

[0102] S2: The lean gas rises to the packing absorption zone 4 and undergoes a second contact treatment with the absorbent liquid material sprinkled by the liquid distributor I5 to obtain clean gas and lean absorbent; and,

[0103] The rich liquid is introduced into the packing desorption section and sprinkled onto the packing desorption zone 15 through the liquid distributor II14. After desorption treatment, rich gas and recycled absorbent for recycling to the packing absorption section and / or the atomizing spray section are obtained;

[0104] S3: The rich gas is extracted through the rich gas extraction port and introduced into the condensation unit 20 for condensation treatment to obtain liquid light hydrocarbons and non-condensable gas;

[0105] S4: The non-condensable gas is returned to the waste gas inlet and introduced into the atomizing spray section together with the VOCs waste gas for the first contact treatment.

[0106] Under this preferred condition, the enrichment efficiency of VOCs is further improved. The non-condensable gas is returned to the waste gas inlet for absorption treatment again, realizing zero emission of non-condensable gas.

[0107] According to some preferred embodiments of the present invention, a vacuum pump 19 is provided between the rich gas extraction port and the condensation unit 20. The vacuum pump 19 is used to extract the rich gas obtained in the packing desorption section and transport it to the condensation unit 20, and maintain the required vacuum degree in the packing desorption section to improve the desorption efficiency of the rich liquid.

[0108] According to a further preferred embodiment of the present invention, as Figure 2 shown, a compressor 25 is further provided between the vacuum pump 19 and the condensation unit 20. The compressor 25 is used to compress the rich gas extracted by the vacuum pump 19, making the rich gas more easily condensed into liquid light hydrocarbons.

[0109] According to some preferred embodiments of the present invention, the condensation unit 20 is also connected to the liquid light hydrocarbon collection unit through a transfer pump 21. The liquid light hydrocarbon collection unit is used to collect and store the liquid light hydrocarbons obtained by condensing the rich gas in the condensation unit, and the transfer pump 21 is used to transport the liquid light hydrocarbons from the condensation unit 20 to the liquid light hydrocarbon collection unit.

[0110] According to some preferred embodiments of the present invention, the recycled absorbent regeneration zone 16 is also independently connected to the atomizing spray unit 10 and the liquid distributor I5 through a recycle pump 17. The recycled absorbent after desorption treatment can be returned to the atomizing spray section and atomized into absorbent droplets by the atomizing spray unit 10 for the first contact treatment with the VOCs waste gas, or can be returned to the packing absorption section and distributed into absorbent liquid material by the liquid distributor I5 for the second contact treatment with the lean gas in the packing absorption zone 4.

[0111] According to some preferred embodiments of the present invention, an automatic control valve III9 is further provided on the connecting pipeline between the circulation pump 17 and the atomizing spray unit 10, and the automatic control valve III9 is used to adjust the flow rate of the circulating absorbent conveyed from the circulating absorbent regeneration zone 16 to the atomizing spray unit 10.

[0112] According to some preferred embodiments of the present invention, an automatic control valve II8 is further provided on the connecting pipeline between the circulation pump 17 and the liquid distributor I5, and the automatic control valve II8 is used to adjust the flow rate of the circulating absorbent conveyed from the circulating absorbent regeneration zone 16 to the liquid distributor I5.

[0113] According to some preferred embodiments of the present invention, a liquid level monitor I13 is further provided in the rich liquid storage area 11, and the rich liquid storage area 11 is connected to the liquid distributor II14 through an automatic control valve I12. In practical applications, to prevent the liquid level of the rich liquid in the rich liquid storage area 11 from being too high, which may cause the atomizing spray unit 10 to be unable to spray absorbent droplets or the contact time between the absorbent droplets and the VOCs waste gas for the first contact treatment to be too short. When the liquid level monitor I13 monitors that the liquid level of the rich liquid in the rich liquid storage area 11 is higher than the set value, the automatic control valve I12 opens, and the rich liquid in the rich liquid storage area 11 is introduced into the liquid distributor II14; when the liquid level monitor I13 monitors that the liquid level of the rich liquid in the rich liquid storage area 11 is lower than the set value, the automatic control valve I12 closes, and the rich liquid storage area 11 stores the rich liquid.

[0114] According to some preferred embodiments of the present invention, a liquid level monitor II24 is further provided in the circulating absorbent regeneration zone 16. In practical applications, when the circulating absorbent in the circulating absorbent regeneration zone 16 is higher than the set value, the circulation pump 17 conveys the circulating absorbent in the circulating absorbent regeneration zone 16 to the atomizing spray unit 10 and / or the liquid distributor I5; when the circulating absorbent in the circulating absorbent regeneration zone 16 is lower than the set value, the circulation pump 17 reduces the conveying amount of the circulating absorbent conveyed to the atomizing spray unit 10 and the liquid distributor I5 or the circulation pump 17 shuts down.

[0115] According to some preferred embodiments of the present invention, a demister I18 is further provided at the rich gas extraction port, and the demister I18 is used to remove the liquid droplets at the rich gas extraction port so that the rich gas can be extracted more smoothly.

[0116] According to some preferred embodiments of the present invention, a demister II6 is further provided at the clean gas discharge port, and the demister II6 is used to remove the liquid droplets at the clean gas discharge port so that the clean gas can be discharged more smoothly.

[0117] According to some preferred embodiments of the present invention, in the atomizing spray section, the waste gas inlet is connected to the waste gas inlet pipeline 1, and the waste gas inlet pipeline 1 is provided with an inlet fan 2, and the inlet fan 2 is used to introduce the VOCs waste gas into the atomizing spray section of the packing tower through the waste gas inlet pipeline 1.

[0118] As Figure 2 shown, according to some preferred embodiments of the present invention, a control valve I22 is further provided on the connecting pipeline between the condensing unit 20 and the waste gas inlet, and the control valve I22 is used to adjust the return rate of the non-condensable gas returned to the waste gas inlet.

[0119] As Figure 2 shown, according to some preferred embodiments of the present invention, a control valve II23 is provided on the clean gas discharge port or the clean gas discharge pipeline 7, and the control valve II23 is used to adjust the discharge rate of the clean gas.

[0120] The third aspect of the present invention provides the application of the aforementioned method and the aforementioned device in waste gas treatment.

[0121] The present invention will be described in detail below through examples. In the following examples, the instruments, reagents, materials, etc. involved, unless otherwise specified, are all conventional instruments, reagents, materials, etc. existing in the prior art and can be obtained through regular commercial channels. The experimental methods, detection methods, etc. involved in the following examples, unless otherwise specified, are all conventional experimental methods, detection methods, etc. existing in the prior art.

[0122] It should be noted that in the present invention, normal temperature means 25 °C and normal pressure means 101 kPa.

[0123] Waste gas I: The concentration of non-methane total VOCs is 500 g / m 3 , based on the total mass of all non-methane VOCs in waste gas I, the content of alkanes is 60 vol%, the content of alkenes is 30 vol%, and the content of aromatic hydrocarbons is 10 vol%. Among them, the alkanes are ethane, propane, butane, pentane, hexane, the alkenes are ethylene, propylene, butene, pentene, and the aromatic hydrocarbons are benzene, toluene, xylene;

[0124] Waste gas II: The concentration of non-methane total VOCs is 500 g / m 3 , based on the total mass of all non-methane VOCs in waste gas I, the content of alkanes is 100 vol%, and among them, the alkanes are ethane, propane, butane, pentane, hexane;

[0125] Waste gas III: The concentration of non-methane total VOCs is 500 g / m 3 , based on the total mass of all non-methane VOCs in waste gas I, the content of alkenes is 100 vol%, and among them, the alkenes are ethylene, propylene, butene, pentene;

[0126] Exhaust gas IV: The concentration of total non-methane VOCs is 500 g / m 3 , based on the total mass of all non-methane VOCs in exhaust gas I, the content of aromatic hydrocarbons is 100 vol%, where the aromatic hydrocarbons are benzene, toluene, and xylene.

[0127] In the following examples, the types of absorbents involved are shown in Table 1 below:

[0128] Table 1

[0129]

[0130] Note: The saturated water content and saturated vapor pressure are measured under normal temperature and pressure conditions.

[0131] In the following examples:

[0132] Exhaust gas treatment device I: As Figure 1 and Figure 2 shown, it includes a packed tower, and the packed tower includes a packing absorption section, an atomizing spray section, and a packing desorption section arranged in sequence from top to bottom. A clean gas discharge port is provided at the top of the packed tower;

[0133] The atomizing spray section includes an atomizing spray unit 10 and a rich liquid accommodation area 11 provided below the atomizing spray unit 10. The atomizing range of the atomizing spray unit 10 is not greater than 1000 μm, and an exhaust gas inlet is also provided between the atomizing spray unit 10 and the rich liquid accommodation area 11;

[0134] The packing absorption section includes a liquid distributor I5 and a packing absorption area 4 provided between the liquid distributor I5 and the atomizing spray unit 10;

[0135] The packing desorption section includes a liquid distributor II14, a packing desorption area 15, and a circulating absorbent regeneration area 16 arranged in sequence from top to bottom. The liquid distributor II14 is provided below the rich liquid accommodation area 11;

[0136] It also includes a condensation unit 20. A rich gas extraction port communicated with the condensation unit 20 is also provided between the liquid distributor II14 and the rich liquid accommodation area 11, and the condensation unit 20 is also communicated with the exhaust gas inlet;

[0137] A vacuum pump 19 is provided between the rich gas extraction port and the condensation unit 20, and a compressor 25 is also provided between the vacuum pump 19 and the condensation unit 20;

[0138] The condensation unit 20 is also communicated with the liquid light hydrocarbon collection unit through a transfer pump 21;

[0139] The cyclic absorbent regeneration zone 16 is also independently communicated with the atomizing spray unit 10 and the liquid distributor I5 through a circulation pump 17;

[0140] The rich liquid containing zone 11 is also provided with a liquid level monitor I13, and the rich liquid containing zone 11 is communicated with the liquid distributor II14 through an automatic control valve I12;

[0141] The cyclic absorbent regeneration zone 16 is also provided with a liquid level monitor II24;

[0142] A demister I18 is also provided at the rich gas extraction port, and a demister II6 is also provided at the clean gas discharge port;

[0143] In the atomizing spray section, the waste gas inlet is communicated with the waste gas inlet pipeline 1, and the waste gas inlet pipeline 1 is provided with an inlet fan 2;

[0144] The packing filled in the packing absorption zone 4 and the packing filled in the packing desorption zone 15 are independently Pall rings, and the Pall rings are purchased from Kelong Petrochemical Equipment Packing Co., Ltd. in Pingxiang City, Jiangxi Province, metal cascade rings, model Φ50.

[0145] Waste gas treatment device II: Similar to the device disclosed in CN205672733U, including:

[0146] An absorption tower, including first to fourth ports;

[0147] A compressor, connected to the first port, for compressing the collected waste gas and discharging it into the absorption tower through the first port;

[0148] An absorbent pump, connected to the second port, for discharging the absorbent into the absorption tower;

[0149] An adsorption tower, connected to the third port of the absorption tower;

[0150] The waste gas enters the absorption tower through the first port, the absorbent enters the absorption tower through the second port, the absorbent and the waste gas flow in opposite directions, and after the waste gas is absorbed, it becomes rich liquid and flows out and is recovered through the fourth port, and the unabsorbed lean gas enters the adsorption tower and is subjected to re-adsorption treatment in the adsorption tower.

[0151] Example 1:

[0152] The waste gas in this example is waste gas I, and this example is carried out in the waste gas treatment device I, including the following steps:

[0153] S1: Introduce the waste gas into the atomizing spray section for the first contact treatment with the absorbent droplets to obtain rich liquid and lean gas;

[0154] S2: Introduce the lean gas into the packed absorption section for a second contact treatment with the absorbent to obtain clean gas and lean liquid; and,

[0155] Introduce the rich liquid into the packed desorption section for desorption treatment to obtain rich gas and a recycled absorbent for recycling to the packed absorption section and / or the atomizing spray section;

[0156] S3: Condense the rich gas to obtain liquid light hydrocarbons and non-condensable gas;

[0157] S4: Return the non-condensable gas to the atomizing spray section for the first contact treatment.

[0158] Specifically, the parameters are as shown in Table 2 below.

[0159] Examples 2 - 5

[0160] Carry out in the manner of Example 1, except that some parameters are changed. Specifically, the parameters are as shown in Table 2 below.

[0161] Comparative Example 1

[0162] Carry out in the manner of Example 1, except that it is carried out in Waste Gas Treatment Device III. Waste Gas Treatment Device III is similar to Waste Gas Treatment Device I, except that the atomizing range of the atomizing spray unit 10 is 1500μm - 2500μm. Specifically, the parameters are as shown in Table 2 below.

[0163] Comparative Example 2

[0164] Carry out in the manner of Example 1, except that the type of absorbent is changed. Specifically, the parameters are as shown in Table 2 below.

[0165] Comparative Example 3

[0166] Carry out in the manner of Example 1, except that the ratio of the inlet volume flow rate of the waste gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent in contact with the lean gas is adjusted. Specifically, the parameters are as shown in Table 2 below.

[0167] Comparative Example 4

[0168] This comparative example is carried out in Waste Gas Treatment Device II and includes the following steps:

[0169] S1: Introduce the waste gas into the absorption tower for a first contact treatment with the absorbent to obtain rich liquid and lean gas;

[0170] S2: Introduce the lean gas into the adsorption tower for a second contact treatment with the absorbent to obtain clean gas and lean liquid;

[0171] Further, subject the rich liquid to desorption treatment to obtain rich gas and a recycled absorbent for recycling to the first contact treatment and / or the second contact treatment;

[0172] S3: Condense the rich gas to obtain liquid light hydrocarbons and non-condensable gas.

[0173] Table 2

[0174]

[0175] Note:

[0176] (1) d1 represents the average particle diameter of the absorbent droplets in step S1;

[0177] (2) Q represents the inlet gas volume flow rate of the waste gas, and L1:L2:L3 represents the inlet gas volume flow rate of the waste gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent in contact with the lean gas;

[0178] (3) T1 represents the temperature of the absorbent droplets in step S1, and T2 represents the temperature of the absorbent in step S2;

[0179] (4) V represents the extraction volume flow rate of the rich gas withdrawn from the packing desorption section in step S3;

[0180] (5) C1 represents the content of VOCs in the clean gas, with the unit of mg / m 3 ; C2 represents the content of VOCs in the rich gas, with the unit of vol%;

[0181] (6) n represents the recovery rate of liquid light hydrocarbons, n = mass of liquid light hydrocarbons / total mass of VOCs in the rich gas;

[0182] (7) Same 1 represents "Same as Example 1".

[0183] Table 2 (continued)

[0184]

[0185] Examples 6 - 8

[0186] The waste gas in this example is waste gas II. This example is carried out in the waste gas treatment device I, and the step method is the same as that in Example 1. Specifically, the various parameters are shown in Table 3 below.

[0187] Examples 9 - 11

[0188] The waste gas in this example is waste gas III. This example is carried out in the waste gas treatment device I, and the step method is the same as that in Example 1. Specifically, the various parameters are shown in Table 3 below.

[0189] Examples 12 - 14

[0190] The waste gas in this embodiment is waste gas IV. This embodiment is carried out in the waste gas treatment device I, and the step method is the same as that in Embodiment 1. Specifically, the parameters are as shown in Table 3 below.

[0191] Table 3

[0192]

[0193] Note:

[0194] (1) d1 represents the average particle diameter of the absorbent droplets described in step S1;

[0195] (2) Q represents the inlet gas volume flow rate of the waste gas, and L1:L2:L3 represents the inlet gas volume flow rate of the waste gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent in contact with the lean gas;

[0196] (3) T1 represents the temperature of the absorbent droplets described in step S1, and T2 represents the temperature of the absorbent described in step S2;

[0197] (4) V represents the extraction volume flow rate of extracting the rich gas from the packing desorption section in step S3;

[0198] (5) C1 represents the content of VOCs in the clean gas, with the unit of mg / m 3 ; C2 represents the content of VOCs in the rich gas, with the unit of vol%;

[0199] (6) n represents the recovery rate of liquid light hydrocarbons, and n = the mass of liquid light hydrocarbons / the total mass of VOCs in the rich gas;

[0200] (7) The same as 1 means "the same as Embodiment 1".

[0201] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solutions of the present invention, including any other suitable combination of each technical feature. These simple modifications and combinations should also be regarded as the content disclosed by the present invention and fall within the protection scope of the present invention.

Claims

1. An exhaust gas treatment method, characterized in that, This method is carried out in an exhaust gas treatment device, which includes a packed tower. The packed tower includes a packed absorption section, an atomizing spray section, and a packed desorption section arranged in sequence from top to bottom; This method includes: S1: Introduce the exhaust gas into the atomizing spray section for the first contact treatment with absorbent droplets to obtain rich liquid and lean gas; S2: Introduce the lean gas into the packed absorption section for the second contact treatment with the absorbent to obtain clean gas and lean liquid; and, Introduce the rich liquid into the packed desorption section for desorption treatment to obtain rich gas and a recycled absorbent for recycling to the packed absorption section and / or the atomizing spray section; Among them, the concentration of total non-methane VOCs in the waste gas is not greater than 1500 g / m 3 ; in step S1, the absorbent droplets are obtained by atomizing the absorbent and / or the lean liquid, and the average particle diameter of the absorbent droplets is not greater than 1000 μm; Wherein, the inlet volume flow rate of the exhaust gas: the spray volume flow rate of the absorbent droplets: the volume flow rate of the absorbent contacting the lean gas = Q: 0.005Q - 0.02Q: 0.005Q - 0.02Q.

2. The method according to claim 1, characterized in that, It also includes the following steps: S3: Condense the rich gas to obtain liquid light hydrocarbons and non-condensable gas; and, Introduce the lean liquid into the atomizing spray section for the first contact treatment with the exhaust gas, or introduce the lean liquid into the packed desorption section for desorption treatment; S4: Return the non-condensable gas to the atomizing spray section for the first contact treatment; Preferably, in step S3, the temperature of the condensation treatment is -120°C to 15°C, and the pressure is 0 - 1 MPa in gauge pressure.

3. The method according to claim 2, wherein Based on the total mass of all non-methane VOCs in the exhaust gas, the content of non-aromatic hydrocarbons is not less than 10 vol%, and the temperature of the condensation treatment is -120°C to 0°C, preferably -30°C to -20°C; And / or, based on the total mass of all non-methane VOCs in the exhaust gas, the content of non-aromatic hydrocarbons is less than 0.5 vol%, and the temperature of the condensation treatment is 3°C to 15°C.

4. The method according to claim 2, characterized in that, In step S3, the rich gas is withdrawn from the packed desorption section and subjected to condensation treatment; Preferably, the withdrawal volume flow rate of the rich gas in step S3: the inlet volume flow rate of the exhaust gas in step S1 = 0.25Q - 0.8Q: Q.

5. The method according to claim 1, wherein In step S2, the pressure of the desorption treatment is -90 kPa to -101 kPa in gauge pressure, and the temperature is 10°C to 50°C.

6. The method according to any one of claims 1-5, characterized in that, In step S1, the absorbent contains a composite component, a hydrogen bond donor, and a hydrogen bond acceptor. The molar ratio of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1:0.5 - 10:0.01 - 0.

2. The hydrogen bond acceptor is selected from at least one of menthol, thymol, lidocaine, and quaternary ammonium salts. The hydrogen bond donor is selected from at least one of fatty acids. The composite component is a mixture of component A and component B. Component A is selected from at least one of p-xylene, methylcyclohexane, dipentene, terpinene, toluene, and n-hexane. Component B is selected from at least one of citronellol, 4-8 saturated monohydric fatty alcohols of C, ethyl benzoate, isophorone, acetic acid, lactic acid, and pyruvic acid; And the saturated vapor pressure of the absorbent at 25°C is not greater than 100 Pa, and the saturated water content is not greater than 2 mol%.

7. The method according to claim 6, wherein Based on the total mass of all non-methane VOCs in the exhaust gas, when the content of alkanes is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents: The molar ratio of the contents of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1: 1 - 4: 0.01 - 0.1; The hydrogen bond acceptor is selected from at least one of menthol, thymol, and lidocaine; The hydrogen bond donor is selected from at least one of saturated fatty acids having C 12-18 and monounsaturated fatty acids having C 12-18 ; The component A is at least one of the p-xylene and the methylcyclohexane, and the component B is at least one of the citronellol and the saturated monohydric aliphatic alcohol of C 4-8 ​ 8. The method according to claim 6, wherein Based on the total mass of all non-methane VOCs in the exhaust gas, when the content of olefins is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents: The molar ratio of the contents of the hydrogen bond acceptor, hydrogen bond donor, and composite component is 1: 1 - 8: 0.01 - 0.2; The hydrogen bond acceptor is selected from at least one of the menthol and the quaternary ammonium bromide; The hydrogen bond donor is selected from at least one of fatty acids with the molecular formula R 1 -COOH, where R 1 is selected from alkyl groups having 6 to 10 carbon atoms, alkenyl groups having 16 carbon atoms; 18 ​ The component A is selected from at least one of the dipentene and the terpinene, and the component B is selected from at least one of the ethyl benzoate and the isophorone.

9. The method according to claim 6, wherein Based on the total mass of all non-methane VOCs in the waste gas, when the content of aromatic hydrocarbons is not less than 50 vol%, the absorbent is selected from at least one of the following absorbents: The molar ratio of the contents of the hydrogen bond acceptor, the hydrogen bond donor, and the composite component is 1:0.5 - 10:0.02 - 0.2; The hydrogen bond acceptor is selected from at least one of the quaternary ammonium salt, the menthol, and the thymol, and the structure of the quaternary ammonium salt is Each R 2 is selected from one of the alkyl groups of C 4-8 and L is Cl or Br; The hydrogen bond donor is selected from at least one of fatty acids with the molecular formula R 3 -COOH, wherein R 3 is C n H 2n+1 or C n H 2n -1, and n is an integer from 5 to 17; The component A is selected from at least one of the toluene and the n-hexane, and the component B is selected from at least one of the acetic acid, the lactic acid, and the pyruvic acid.

10. The method according to any one of claims 1-5, characterized in that In step S1, the temperature of the absorbent droplets is 10°C - 50°C; And / or, in step S2, the temperature of the absorbent is 10°C - 50°C.

11. The method according to any one of claims 1-5, characterized in that, In step S2, the packing filled in the packing absorption section is at least one of the perforated plate corrugated packing, the plate corrugated packing, the wire mesh corrugated packing, the Raschig ring, the Pall ring, and the theta ring; And / or, the packing filled in the packing desorption section is at least one of the perforated plate corrugated packing, the plate corrugated packing, the wire mesh corrugated packing, the Raschig ring, the Pall ring, and the theta ring.

12. The method according to any one of claims 1-5, characterized in that, A clean gas discharge port is provided at the top of the packed tower; The atomizing spray section includes an atomizing spray unit (10) and a rich liquid accommodation area (11) provided below the atomizing spray unit (10). The atomizing range of the atomizing spray unit (10) is not greater than 1000 μm, and an exhaust gas inlet is further provided between the atomizing spray unit (10) and the rich liquid accommodation area (11); The packing absorption section includes a liquid distributor I (5) and a packing absorption area (4) provided between the liquid distributor I (5) and the atomizing spray unit (10); The packing desorption section includes a liquid distributor II (14), a packing desorption area (15), and a circulating absorbent regeneration area (16) arranged in sequence from top to bottom. The liquid distributor II (14) is provided below the rich liquid accommodation area (11); 13. The method according to claim 12, wherein The waste gas treatment device further includes a condensation unit (20). A rich gas extraction port communicated with the condensation unit (20) is further provided between the liquid distributor II (14) and the rich liquid accommodation area (11), and the condensation unit (20) is also communicated with the exhaust gas inlet; 14. The method according to claim 12, wherein The circulating absorbent regeneration area (16) is also independently communicated with the atomizing spray unit (10) and the liquid distributor I (5) through a circulating pump (17); 15. An exhaust gas treatment device, characterized in that, It includes a packed tower. The packed tower includes a packing absorption section, an atomizing spray section, and a packing desorption section arranged in sequence from top to bottom. A clean gas discharge port is provided at the top of the packed tower; The atomizing spray section includes an atomizing spray unit (10) and a rich liquid accommodation area (11) provided below the atomizing spray unit (10). The atomizing range of the atomizing spray unit (10) is not greater than 1000 μm, and an exhaust gas inlet is further provided between the atomizing spray unit (10) and the rich liquid accommodation area (11); The packing absorption section includes a liquid distributor I (5) and a packing absorption zone (4) provided between the liquid distributor I (5) and the atomizing spray unit (10); The packing desorption section includes a liquid distributor II (14), a packing desorption zone (15), and a circulating absorbent regeneration zone (16) arranged in sequence from top to bottom. The liquid distributor II (14) is provided below the rich liquid storage area (11).

16. The device according to claim 15, characterized in that, The waste gas treatment device further includes a condensation unit (20). A rich gas extraction port communicating with the condensation unit (20) is also provided between the liquid distributor II (14) and the rich liquid storage area (11), and the condensation unit (20) is also connected to the waste gas inlet.

17. The device according to claim 16, wherein A vacuum pump (19) is provided between the rich gas extraction port and the condensation unit (20); Preferably, a compressor (25) is also provided between the vacuum pump (19) and the condensation unit (20).

18. The device according to claim 16, characterized in that, The condensation unit (20) is also connected to the liquid light hydrocarbon collection unit through a transfer pump (21).

19. The device according to claim 15, characterized in that, The circulating absorbent regeneration zone (16) is also independently connected to the atomizing spray unit (10) and the liquid distributor I (5) through a circulating pump (17).

20. The device according to claim 15, characterized in that, The rich liquid storage area (11) is also provided with a liquid level monitor I (13), and the rich liquid storage area (11) is connected to the liquid distributor II (14) through an automatic control valve I (12).

21. The device according to claim 15, characterized in that, The circulating absorbent regeneration zone (16) is also provided with a liquid level monitor II (24).

22. The device according to any one of claims 15 - 21, characterized in that, A demister I (18) is also provided at the rich gas extraction port; and / or, a demister II (6) is also provided at the clean gas discharge port.

23. The device according to any one of claims 15-21, characterized in that, In the atomizing spray section, the waste gas inlet is connected to a waste gas inlet pipeline (1), and an inlet fan (2) is provided on the waste gas inlet pipeline (1).

24. Use of the method according to any one of claims 1 - 14 and / or the device according to any one of claims 15 - 23 in waste gas treatment.

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