CN211799844U - Aromatic hydrocarbon tank field oil gas step recovery processing system - Google Patents
Aromatic hydrocarbon tank field oil gas step recovery processing system Download PDFInfo
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Abstract
The utility model discloses an aromatic hydrocarbon tank field oil gas step recovery processing system, include: the device comprises an aromatic hydrocarbon storage tank, a C4+ adsorption/desorption tower, a C4+ desorption gas condenser, a mixed aromatic hydrocarbon tank, a C2+ adsorption/desorption tower and a non-condensable gas treatment device, wherein the aromatic hydrocarbon storage tank, the C4+ adsorption/desorption tower and the C2+ adsorption/desorption tower are sequentially connected, the C4+ desorption gas condenser is respectively connected with the C4+ adsorption/desorption tower and the mixed aromatic hydrocarbon tank, and the non-condensable gas treatment device is connected with the C2+ adsorption/desorption tower. The aromatic hydrocarbon tank area oil gas step recovery processing system has the beneficial effects of high aromatic hydrocarbon product adsorption efficiency and contribution to environmental protection.
Description
Technical Field
The utility model relates to a chemical industry field especially relates to an aromatic hydrocarbon tank field oil gas step recovery processing system.
Background
Generally, oil gas products generated in an aromatic hydrocarbon tank area in a petrochemical refinery comprise various oil products and aromatic hydrocarbon (benzene, toluene, xylene and the like) volatile matters, and the traditional oil gas treatment process of the aromatic hydrocarbon tank area adsorbs the various volatile products and then carries out emission treatment. However, due to the characteristic of similar compatibility, oil and gas products usually contain various hydrocarbons with carbon atoms from 1 to 10, and uniform condensation and efficient adsorption cannot be realized, particularly, the adsorption difficulty is higher for the hydrocarbons with lower carbon atoms, so that a large amount of C2-C3 hydrocarbons still remain in the gas discharged after adsorption, and the direct discharge of C2-C3 hydrocarbons can cause environmental pollution. Therefore, the traditional oil gas treatment process of the aromatic hydrocarbon tank area has the technical problems of low aromatic hydrocarbon product adsorption efficiency and environmental pollution.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide an aromatic hydrocarbon tank field oil gas step recovery processing system to overcome the technical problem of aromatic hydrocarbon result adsorption efficiency low, the polluted environment that traditional aromatic hydrocarbon tank field oil gas treatment process exists.
To achieve the purpose, the utility model adopts the following technical proposal:
an aromatic hydrocarbon tank field oil gas cascade recovery processing system includes: the device comprises an aromatic hydrocarbon storage tank, a C4+ adsorption/desorption tower, a C4+ desorption gas condenser, a mixed aromatic hydrocarbon tank, a C2+ adsorption/desorption tower and a non-condensable gas treatment device, wherein the aromatic hydrocarbon storage tank, the C4+ adsorption/desorption tower and the C2+ adsorption/desorption tower are sequentially connected, the C4+ desorption gas condenser is respectively connected with the C4+ adsorption/desorption tower and the mixed aromatic hydrocarbon tank, and the non-condensable gas treatment device is connected with the C2+ adsorption/desorption tower.
In one embodiment, the C4+ adsorption/desorption tower is filled with carbon nano-adsorbent.
In one embodiment, the C2+ adsorption/desorption tower is filled with a micro-nano composite adsorbent.
In one embodiment, the aromatic hydrocarbon tank field oil gas cascade recovery processing system further comprises a pressure boosting device, and the pressure boosting device is arranged between the aromatic hydrocarbon storage tank and the C4+ adsorption/desorption tower.
In one embodiment, the non-condensable gas processing device is also connected with the C4+ desorption gas condenser.
In one embodiment, the non-condensable gas processing device is a carbonization device.
In one embodiment, the non-condensable gas processing device is an oxidation device.
In one embodiment, the number of the C4+ adsorption/desorption towers is not less than two.
In one embodiment, the number of the C2+ adsorption/desorption towers is not less than two.
The aromatic hydrocarbon tank area oil gas step recovery processing system comprises an aromatic hydrocarbon storage tank, a C4+ adsorption/desorption tower, a C4+ desorption gas condenser, a mixed aromatic hydrocarbon tank, a C2+ adsorption/desorption tower and a non-condensable gas processing device. Wherein, the arene storage tank is used for storing the oil gas in the arene tank field. The C4+ adsorption/desorption tower is connected with the aromatic hydrocarbon storage tank and is used for condensing and adsorbing C4+ products in oil gas in the aromatic hydrocarbon tank area, desorbing and vaporizing the liquid phase C4+ products obtained by adsorption and sending the liquid phase C4+ products into a C4+ desorption gas condenser. The C4+ desorption gas condenser is connected with the C4+ adsorption/desorption tower and is used for condensing and liquefying the aromatic hydrocarbon oil gas obtained by vaporization of the C4+ adsorption/desorption tower to obtain a liquid aromatic hydrocarbon mixture and sending the liquid aromatic hydrocarbon mixture into the mixed aromatic hydrocarbon tank. And the mixed aromatic hydrocarbon tank and a C4+ desorption gas condenser are used for storing the liquid aromatic hydrocarbon mixture. The C2+ adsorption/desorption tower 50 is connected with the C4+ adsorption/desorption tower and is used for condensing and adsorbing the oil gas in the aromatic hydrocarbon tank area after condensation and adsorption by the C4+ adsorption/desorption tower, adsorbing C2-C3 hydrocarbons in the oil gas in the aromatic hydrocarbon tank area, desorbing and vaporizing the liquid-phase C2-C3 hydrocarbons obtained by adsorption and sending the hydrocarbons into a noncondensable gas treatment device. The non-condensable gas treatment device is connected with the C2+ adsorption/desorption tower and is used for carrying out harmless treatment or recycling treatment on C2-C3 hydrocarbons obtained by vaporization of the C2+ adsorption/desorption tower.
The aromatic hydrocarbon tank area oil gas cascade recovery processing system carries out cascade processing on the oil gas in the aromatic hydrocarbon tank area aiming at the current situation that the concentration and the adsorption characteristics of different hydrocarbons have great difference, firstly carries out complete adsorption on C4+ hydrocarbons, and then realizes efficient adsorption on C2-C3 hydrocarbons. And the adsorbed C4+ hydrocarbons are subjected to high-temperature desorption and re-cooling to be changed into a pure hydrocarbon liquid mixture, and the pure hydrocarbon liquid mixture is sent to a mixed aromatic hydrocarbon tank and is periodically sent to a separation tower to realize recovery. The adsorbed light hydrocarbon (C2-C3 hydrocarbon) is desorbed and then is subjected to innocent treatment or recycling treatment. The aromatic hydrocarbon tank area oil gas step recovery processing system can realize complete adsorption of C4+ hydrocarbons and efficient adsorption of C2-C3 hydrocarbons, has high adsorption efficiency of aromatic hydrocarbon products, can realize online desorption and recycling of C4+ hydrocarbon substances, and realize online desorption and oxidation discharge of C2-C3 hydrocarbons, has high recycling efficiency of C4+ hydrocarbons, does not pollute the environment, and is beneficial to environmental protection.
Drawings
FIG. 1 is a schematic diagram of a step recovery processing system for oil and gas in an aromatic hydrocarbon tank field in one embodiment.
Description of reference numerals:
10-aromatic hydrocarbon storage tank, 20-C4+ adsorption/desorption tower, 30-C4+ desorption gas condenser, 40-mixed aromatic hydrocarbon tank, 50-C2+ adsorption/desorption tower, 60-noncondensable gas treatment device and 70-supercharging device.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplification of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Referring to fig. 1, an embodiment of a gradient oil gas recovery processing system for an aromatic hydrocarbon tank area includes an aromatic hydrocarbon storage tank 10, a C4+ adsorption/desorption tower 20, a C4+ desorption gas condenser 30, a mixed aromatic hydrocarbon tank 40, a C2+ adsorption/desorption tower 50, and a noncondensable gas processing apparatus 60, the aromatic hydrocarbon storage tank 10, the C4+ adsorption/desorption tower 20, and the C2+ adsorption/desorption tower 50 are sequentially connected, the C4+ desorption gas condenser 30 is respectively connected to the C4+ adsorption/desorption tower 20 and the mixed aromatic hydrocarbon tank 40, and the noncondensable gas processing apparatus 60 is connected to the C2+ adsorption/desorption tower 50.
Specifically, the aromatics storage tank 10 is used to store aromatics tank field oil and gas. The C4+ adsorption/desorption tower 20 is connected with the aromatic hydrocarbon storage tank 10 and is used for condensing and adsorbing C4+ products in oil gas in the aromatic hydrocarbon storage tank area, desorbing and vaporizing the liquid phase C4+ products obtained by adsorption and sending the liquid phase C4+ products into a C4+ desorption gas condenser 30. The C4+ desorption gas condenser 30 is connected with the C4+ adsorption/desorption tower 20 and is used for condensing and liquefying the aromatic hydrocarbon oil gas obtained by vaporizing the C4+ adsorption/desorption tower 20 to obtain a liquid aromatic hydrocarbon mixture and sending the liquid aromatic hydrocarbon mixture into the mixed aromatic hydrocarbon tank 40. The mixed aromatics tank 40 and the C4+ desorption gas condenser 30 are used for storing the liquid aromatics mixture. The C2+ adsorption/desorption tower 50 is connected with the C4+ adsorption/desorption tower 20 and is used for condensing and adsorbing the oil gas in the aromatic hydrocarbon tank area after being condensed and adsorbed by the C4+ adsorption/desorption tower 20, adsorbing C2-C3 hydrocarbons in the oil gas in the aromatic hydrocarbon tank area, desorbing and vaporizing the liquid-phase C2-C3 hydrocarbons obtained through adsorption and sending the hydrocarbons into the noncondensable gas treatment device 60. The non-condensable gas treatment device 60 is connected with the C2+ adsorption/desorption tower 50 and is used for carrying out harmless treatment or recycling treatment on C2-C3 hydrocarbons obtained by vaporization of the C2+ adsorption/desorption tower 50.
Further, in one embodiment, the noncondensable gas treatment device 60 is further connected to the C4+ desorption gas condenser 30, and the noncondensable gas treatment device 60 is further configured to perform a harmless treatment or a recycling treatment on the C4+ desorption gas (less condensable substances such as C4-C5).
In one embodiment, the noncondensable gas treatment device 60 is a carbonization device, and the carbonization device reuses the C2-C3 hydrocarbons and the C4+ desorption gas obtained by vaporizing the C2+ adsorption/desorption tower 50. Specifically, the carbonization device vaporizes C2+ adsorption/desorption tower 50 through an induced draft fan to obtain C2-C3 hydrocarbons and C4+ desorption gas, the C2-C3 hydrocarbon gases and the C4+ desorption gas are changed into carbon on a catalyst at the temperature of 500 plus materials and 800 ℃, methane and a small amount of hydrogen are generated, the methane and the small amount of hydrogen with certain temperature are cooled and then are merged into an outlet of the C2+ adsorption/desorption tower 50 to be discharged, the carbonized tail gas is cooled through indirect heat exchange and is directly discharged to the atmosphere, the carbon obtained through carbonization can be discharged from the non-condensable gas treatment device 60 to be recovered, and the recovered carbon can be used for manufacturing carbon nano-adsorbent.
In one embodiment, the noncondensable gas treatment device 60 is an oxidation device, and the oxidation device performs harmless treatment on the C2-C3 hydrocarbons and the C4+ desorption gas obtained by vaporizing the C2+ adsorption/desorption tower 50. Specifically, the oxidation device carries out catalytic oxidation on C2-C3 hydrocarbons and C4+ desorption gas obtained by vaporizing C2+ adsorption/desorption tower 50, and converts the C2-C3 hydrocarbons and the C4+ desorption gas into CO2And water discharge.
In one embodiment, the aromatics tank field oil gas cascade recycling processing system further comprises a pressure boosting device 70, and the pressure boosting device 70 is arranged between the aromatics storage tank 10 and the C4+ adsorption/desorption tower 20. In this embodiment, a pressurizing device 70 is disposed between the aromatic hydrocarbon storage tank 10 and the C4+ adsorption/desorption tower 20, and the pressure of the oil gas in the aromatic hydrocarbon tank area is first pressurized to 0.001MPa-2.0MPa to adapt to the following adsorption and desorption processes. After the oil gas in the aromatic hydrocarbon tank area is pressurized, the gas speed can be slowed down, the adsorption time can be prolonged, and the adsorption rate can be improved. And, through carrying out pressurization processing to arene jar district oil gas, also can increase the operational flexibility of handling oil gas.
Specifically, considering that the oil gas is mainly a mixture of nitrogen and hydrocarbon, the C4+ adsorption/desorption tower 20 adopts a high-efficiency cooling adsorption tower, is provided with a jacket and a coil pipe in the tower, an adsorbent filling layer is filled in contact with the coil pipe, the adsorbent adopts a carbon nano adsorbent, the carbon nano adsorbent has good adsorption rate and desorption rate to C4+ hydrocarbon, the maximum liquid adsorption rate is 1.5 times of the adsorbent amount, and the desorption rate at about 90-200 ℃ can reach 100%. The C4+ adsorption/desorption tower 20 indirectly exchanges heat through a cooling medium (a cooling medium with the temperature of 5-10 ℃ is provided by utilizing a self-contained refrigerating device), the temperature in the cooling adsorption tower is kept at 10-15 ℃, so that C4+ hydrocarbons (namely C4-C10 hydrocarbons) are condensed on the carbon nano adsorbent, the cooling effect of the equipment is better as the liquid phase increases, the equipment is quickly transited to a gas balance composition under an operation temperature, the partial pressure of the C4+ hydrocarbons in nitrogen is greatly reduced, after adsorption saturation, a jacket of the C4+ adsorption/desorption tower 20 and a heat exchange tube are filled with steam to heat the C4+ adsorption/desorption tower 20 to 100-200 ℃, aromatic hydrocarbons on the carbon nano adsorbent are evaporated, aromatic hydrocarbon oil gas evaporated is sent to a C4+ desorption gas condenser 30, the aromatic hydrocarbon oil gas enters a mixed aromatic hydrocarbon tank 40 after passing through the C4+ desorption gas condenser 30, periodically sent to a separation tower for recovery. Furthermore, in the process of condensing and liquefying the aromatic hydrocarbon oil gas in the C4+ desorption gas condenser 30, substances which are not easy to condense, such as C4-C5 hydrocarbons, form desorption gas, and the desorption gas is discharged from the top of the C4+ desorption gas condenser 30 and sent to the non-condensable gas treatment device 60 for harmless treatment or recycling treatment.
The oil gas in the aromatic hydrocarbon tank area after condensation and adsorption in the C4+ adsorption/desorption tower 20 enters the C2+ adsorption/desorption tower 50 and then is subjected to condensation and adsorption treatment on C2-C3 hydrocarbons, the oil gas in the aromatic hydrocarbon tank area passes through a C2-C3 hydrocarbon adsorbent layer in the C2+ adsorption/desorption tower 50, C2-C3 hydrocarbon adsorbent layer adsorbs C2-C3 hydrocarbons, and then the gas at the outlet of the C2+ adsorption/desorption tower 50 is discharged up to the standard, and specifically, the C2-C3 hydrocarbon adsorbent adopts a micro-nano composite adsorbent. Further, after the C2-C3 hydrocarbon adsorbent layer is saturated in adsorption, steam is introduced into a jacket of the C2+ adsorption/desorption tower 50 and a heat exchange pipe to heat the C2+ adsorption/desorption tower 50 to 90-200 ℃, C2-C3 hydrocarbon and water on the micro-nano composite adsorbent are sequentially driven out and sent to the non-condensable gas treatment device 60 for harmless treatment or recycling treatment.
In one embodiment, the number of the C4+ adsorption/desorption columns 20 is not less than two in order to improve the adsorption/desorption efficiency of the C4+ hydrocarbons. As shown in fig. 1, in this embodiment, two C4+ adsorption/desorption towers 20 with the same function are provided, one C4+ adsorption/desorption tower 20 is switched to another C4+ adsorption/desorption tower 20 for adsorption after being saturated in adsorption, the C4+ adsorption/desorption tower 20 which is saturated in adsorption is switched to a desorption mode, and the switching operation of the two C4+ adsorption/desorption towers 20 can save the adsorption/desorption waiting time and improve the adsorption/desorption efficiency of C4+ hydrocarbons. The switching of the two C4+ adsorption/desorption towers 20 is based on that a certain liquid level appears on a tower bottom viewing mirror or a hydraulic pipe, and the content of C4 and C4+ total hydrocarbons in outlet gas is close to 80-85% of the highest value of qualified emission. The two C4+ adsorption/desorption columns 20 are switched between a cooling medium and a heating medium, and are controlled by a DCS (Distributed Control System) System. When the C4+ adsorption/desorption tower 20 adsorbs, the heating medium channel is closed, the cooling medium channel is opened, and the cooling medium is pumped in and circulated by the refrigerator, so that the C4+ adsorption/desorption tower 20 is cooled. In the process, residual heat medium in the heating coil is automatically cooled, the volume is shrunk, and the safe operation can be realized. During desorption, the heating medium channel is opened, and the cooling medium channel is gradually closed. In this process, as the C4+ adsorption/desorption column 20 is heated, the medium in the cooling coil is also heated, corresponding to a certain partial pressure. Therefore, the cooling medium valve cannot be completely closed to ensure that the pressure of the cooling medium in the coil pipe does not rise, and part of vaporized cooling medium enters the refrigerator and then is naturally cooled, so that the refrigerator can be safely operated. In this embodiment, two C4+ adsorption/desorption towers 20 are provided, and in other embodiments, the number of C4+ adsorption/desorption towers 20 may be more than two according to the actual process requirement, and this embodiment is not particularly limited.
In one embodiment, the number of the C2+ adsorption/desorption columns 50 is not less than two in order to improve the adsorption/desorption efficiency of the C2-C3 hydrocarbons. As shown in fig. 1, in this embodiment, two C2+ adsorption/desorption towers 50 having the same function are provided, and when one C2+ adsorption/desorption tower 50 is saturated in adsorption, the other C2+ adsorption/desorption tower 50 is switched to perform adsorption. The basis for switching operation of the two C2+ adsorption/desorption columns 50 is: the non-methane total hydrocarbon content in the outlet gas is close to 85-99% of the maximum acceptable emissions value. The two C2+ adsorption/desorption towers 50 are switched between cooling media and heating media and are controlled by a DCS (distributed control system). In this embodiment, two C2+ adsorption/desorption towers 50 are provided, and in other embodiments, the number of C2+ adsorption/desorption towers 50 may be more than two according to the actual process requirement, and this embodiment is not particularly limited.
In one embodiment, the number of the noncondensable gas treatment devices 60 may be not less than two to improve the carbonization or oxidation efficiency. As shown in fig. 1, in the present embodiment, the number of the noncondensable gas treatment devices 60 is two. The two noncondensable gas treatment devices 60 may be both carbonization devices or both oxidation devices, and when the pressure drop of one of the noncondensable gas treatment devices 60 becomes large, switching is performed to improve the treatment efficiency of the noncondensable gas. Specifically, the noncondensable gas treatment device 60 has a small size, and is switched by directly replacing after cutting. Of course, in other embodiments, one of the two non-condensable gas treatment devices 60 may be an oxidation device, and the other may be a carbonization device, and the oxidation device and the carbonization device may be switched to operate alternately according to specific process requirements to perform harmless treatment or reuse treatment on the non-condensable gas. Further, the number of the noncondensable gas treatment devices 60 may be more than two according to the actual process requirement, and the above embodiment is not particularly limited.
The operation process of the aforementioned oil gas cascade recycling system in the aromatic hydrocarbon tank field is specifically described below with reference to fig. 1: firstly, the oil gas in the aromatic hydrocarbon tank area stored in the aromatic hydrocarbon storage tank 10 is pressurized by a pressurizing device 70 and then enters one C4+ adsorption/desorption tower 20, after the C4+ adsorption/desorption tower 20 is saturated by adsorption, the other C4+ adsorption/desorption tower 20 is switched to adsorb, meanwhile, the aromatic hydrocarbon oil in the C4+ adsorption/desorption tower 20 which is saturated by adsorption is evaporated, the evaporated aromatic hydrocarbon oil gas is sent to a C4+ desorption gas condenser 30, the aromatic hydrocarbon oil gas is condensed and liquefied by the C4+ desorption gas condenser 30 and then enters a mixed aromatic hydrocarbon tank 40 and is periodically sent to a separation tower to be recovered, the desorbed gas is discharged from the top of the C4+ desorption gas condenser 30 and then sent to a non-condensable gas processing device 60 for harmless treatment or reutilization treatment, and a small amount of residual desorbed gas tail gas is directly discharged. The oil gas in the aromatic hydrocarbon tank area condensed and adsorbed by the C4+ adsorption/desorption tower 20 enters one C2+ adsorption/desorption tower 50, the gas at the outlet of the C2+ adsorption/desorption tower 50 is discharged after the oil gas in the aromatic hydrocarbon tank area is adsorbed by the micro-nano composite adsorbent, after the adsorbent layer of the C2-C3 hydrocarbon adsorbent is saturated, the other C2+ adsorption/desorption tower 50 is switched to adsorb, and the C2+ C2-C3 hydrocarbon and water in the adsorption/desorption tower 50 which are adsorbed and saturated are sequentially expelled to be sent to one non-condensable gas treatment device 60 to be subjected to harmless treatment or reutilization treatment, and when the pressure drop of the non-condensable gas treatment device 60 is increased, the other non-condensable gas treatment device 60 is switched to be subjected to carbonization/oxidation treatment. Further, the desorbed gas generated by the C4+ desorbing gas condenser 30 is sent to the noncondensable gas treatment device 60 for harmless treatment or recycling treatment.
The aromatic hydrocarbon tank area oil gas cascade recovery processing system carries out cascade processing on the oil gas in the aromatic hydrocarbon tank area aiming at the current situation that the concentration and the adsorption characteristics of different hydrocarbons have great difference, firstly carries out complete adsorption on C4+ hydrocarbons, and then realizes efficient adsorption on C2-C3 hydrocarbons. And the adsorbed C4+ hydrocarbons are subjected to high-temperature desorption and re-cooling to be changed into a pure hydrocarbon liquid mixture, and the pure hydrocarbon liquid mixture is sent to a mixed aromatic hydrocarbon tank and is periodically sent to a separation tower to realize recovery. The adsorbed light hydrocarbon (C2-C3 hydrocarbon) is desorbed and then is subjected to innocent treatment or recycling treatment. The aromatic hydrocarbon tank area oil gas cascade recovery processing system can realize complete adsorption of C4+ hydrocarbons and efficient adsorption of C2-C3 hydrocarbons, has high adsorption efficiency of aromatic hydrocarbon products, can realize online desorption and recycling of C4+ hydrocarbon substances, and can realize online desorption and harmless treatment or recycling treatment of C2-C3 hydrocarbons, has high recycling efficiency of C4+ hydrocarbons, cannot cause pollution to the environment, and is beneficial to environmental protection.
The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (9)
1. The utility model provides an aromatic hydrocarbon tank field oil gas cascade recovery processing system which characterized in that includes: the device comprises an aromatic hydrocarbon storage tank (10), a C4+ adsorption/desorption tower (20), a C4+ desorption gas condenser (30), a mixed aromatic hydrocarbon tank (40), a C2+ adsorption/desorption tower (50) and a non-condensable gas treatment device (60), wherein the aromatic hydrocarbon storage tank (10), the C4+ adsorption/desorption tower (20) and the C2+ adsorption/desorption tower (50) are sequentially connected, the C4+ desorption gas condenser (30) is respectively connected with the C4+ adsorption/desorption tower (20) and the mixed aromatic hydrocarbon tank (40), and the non-condensable gas treatment device (60) is connected with the C2+ adsorption/desorption tower (50).
2. The aromatics drum hydrocarbon cascade recycling process system of claim 1, wherein the C4+ adsorption/desorption column (20) is filled with carbon nano-adsorbent.
3. The aromatics tank field oil and gas step recovery processing system of claim 1, wherein the C2+ adsorption/desorption column (50) is filled with micro-nano composite adsorbent.
4. The aromatics tank field hydrocarbon cascade recovery processing system of claim 1, further comprising a pressure boosting device (70), the pressure boosting device (70) disposed between the aromatics storage tank (10) and the C4+ adsorption/desorption column (20).
5. The aromatics drum hydrocarbon cascade recovery processing system of claim 1, wherein the non-condensable gas processing device (60) is further connected to the C4+ desorber condenser (30).
6. The aromatics drum field hydrocarbon cascade recovery processing system of claim 5, wherein the non-condensable gas processing apparatus (60) is a carbonization apparatus.
7. The aromatics drum field hydrocarbon cascade recovery processing system of claim 5, wherein the non-condensable gas processing apparatus (60) is an oxidizer.
8. The aromatics drum field hydrocarbon cascade recovery processing system of any one of claims 1-7, characterized in that the number of C4+ adsorption/desorption columns (20) is not less than two.
9. The aromatics drum field hydrocarbon cascade recovery processing system of any one of claims 1-7, characterized in that the number of C2+ adsorption/desorption columns (50) is not less than two.
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