Pressurized absorption and adsorption oil gas recovery process

Abstract

The invention discloses a pressurized absorption and adsorption oil gas recovery process, and particularly relates to the technical field of oil gas recovery. The oil gas recovery process comprises the following steps: raw material oil gas is boosted by a compressor and then enters an absorption tower, then is absorbed by absorption oil, organic matters are absorbed by the absorption oil and flow out of a device along with rich absorption oil, and non-condensable gas at the tower top enters an adsorption bed group at 0-50 DEG C for adsorption separation; the adsorption beds in the adsorption bed group are sequentially subjected to the following steps: an adsorption step and regeneration operation steps including reverse release, vacuum pumping, vacuum cleaning, reverse charging and the like on the adsorption beds. Compared with a normal-pressure adsorption process, the process disclosed by the invention is easier to obtain tail gas with extremely low non-methane hydrocarbon concentration and has high organic matter recovery rate. Researches show that the higher the raw oil gas concentration is, the lighter the oil gas components are, the larger the oil gas recovery scale is, and the more obvious advantages of the process are.

Description

Technical Field

[0001] The invention belongs to the technical field of oil and gas recovery, and specifically relates to a pressurized absorption and adsorption oil and gas recovery process. Background Art

[0002] Light oil products with saturated vapor pressure above 5kPa, such as crude oil, gasoline, naphtha, condensate oil, stable light hydrocarbons, etc., or light chemicals, such as benzene, toluene, methyl tert-butyl ether (MTBE), methanol, propylene oxide, etc., and organic liquids containing the above light oil products or light chemicals, hereinafter collectively referred to as "light oil products", will displace oil and gas with a volume flow rate slightly greater than the volume flow rate of the loaded liquid during the process of loading and loading (hereinafter collectively referred to as "loading"). At the loading temperature, the organic matter concentration in the oil and gas is usually 5-50v%, and the rest is mainly inert gas components such as nitrogen or air. Under normal circumstances, for every 1t of light oil loaded, the loss of organic matter is about 0.1-1.2kg. Of course, the present invention is also applicable to oil and gas of similar concentration and composition produced in other process. The oil and gas loss during the loading process of light oil products is large and the concentration is high, which not only causes a large amount of organic resource loss, but also seriously pollutes the atmospheric environment, and is the focus of volatile organic compounds (VOCs) control.

[0003] The main function of oil and gas recovery is to liquefy and recover the organic matter in the oil and gas, and discharge the qualified tail gas directly into the atmosphere, so as to achieve the dual purpose of recovering organic resources and protecting the environment. Therefore, it is the best way to control VOCs. In the national or local relevant standards for oil and gas recovery in China, the emission tail gas indicators currently implemented in most fields such as petrochemicals, coal chemical industry, oil field development, and chemical industry are: non-methane total hydrocarbons <120mg / m 3 , the organic matter recovery rate is greater than 95%; and the Ministry of Environmental Protection’s latest "Technical Guidelines for Emergency Emission Reduction in Key Industries during Heavy Pollution Weather (2020 Revised Edition)" (Environmental Office Atmospheric Letter

[2020] No. 340) requires that the exhaust gas index be controlled at non-methane total hydrocarbons <60mg / m 3 (This invention refers to this type of tail gas non-methane total hydrocarbon concentration control index as "mg-level compliance"). In the field of VOCs treatment in oil storage depots and docks, due to the lack of advanced and feasible high-standard oil and gas recovery technology, the tail gas emission index implemented is: non-methane total hydrocarbon <25g / m 3 , organic matter recovery rate>95% (this invention refers to this type of tail gas concentration control index as "g-level standard"). However, from the development trend, it is a general trend for VOCs management fields such as oil storage depots and docks to upgrade oil and gas recovery emission indicators to "mg-level standard". For high-concentration oil and gas recovery such as light oil loading, when the tail gas concentration of non-methane total hydrocarbons <120mg / m 3When the organic matter recovery rate is greater than 99.9%, it is very close to the VOCs treatment limit, so it is very ideal and challenging.

[0004] The adsorption oil and gas recovery process is the mainstream process for oil and gas recovery loaded with light oil products at home and abroad. Its main process flow is to separate oil and gas by adsorption at normal temperature and pressure, adsorb organic components with strong adsorption force on the adsorbent, and discharge inert gas components with weak adsorption force as qualified tail gas; when the adsorbent reaches a certain adsorption saturation, switch the operation, regenerate the adsorption bed, and desorb the organic matter adsorbed on the adsorbent from the adsorbent through vacuuming and other operation steps, so that the adsorbent can restore its adsorption activity, and obtain concentrated organic desorbed gas at the same time, and finally absorb the desorbed gas with light oil products, and absorb and liquefy the recovered organic matter into the absorption oil. However, since it is adsorbed and absorbed at normal pressure, the defects of this process are obvious when dealing with high-concentration oil and gas containing light components. First, the volume flow rate of the adsorption operation is large, so the size of the equipment and pipeline valves is large, resulting in a large footprint; second, the amount of organic matter brought into the adsorption bed by oil and gas is large, and the adsorption and regeneration load is large, which leads to large investment and energy consumption in the adsorption and regeneration system of the device; third, the concentration of oil and gas entering the adsorption bed is high, resulting in significantly higher adsorption hotspot temperatures of the adsorption bed, and the hotspot temperature often exceeds 85°C, which brings risks to the operation safety of the adsorption bed. The latest national standard "Technical Standard for Oil and Gas Recovery and Treatment Facilities" GBT 50759-2022 stipulates that the adsorption bed temperature should not be higher than 60°C; third, because the oil and gas contain light components, the tail gas concentration of this process of foreign technology can usually only meet the non-methane total hydrocarbons <10g / m 3 To meet the requirements, if we want to further reduce the exhaust gas concentration, the investment and energy consumption will increase significantly.

[0005] Patent application number CN 205913968 U proposes an oil and gas recovery device for pressurized absorption and adsorption process, including an absorption tower, a compressor, an oil supply pump, an absorption tower and an oil return pump, wherein the compressor is connected to the air inlet of the absorption tower, the oil supply pump is connected to the liquid inlet of the absorption tower, the oil return pump is connected to the oil and liquid outlet of the absorption tower, and the absorption tower is connected to the air outlet of the absorption tower. The further technical solution of the patent includes: using a liquid ring compressor, the absorption and adsorption pressure conditions are 0.2-0.3MPa; the adsorption tower includes a first adsorption zone, a second adsorption zone and a partition plate, the partition plate is arranged between the first adsorption zone and the second adsorption zone, and the adsorbents filled in the first adsorption zone and the second adsorption zone are molecular sieves and activated carbon; the adsorbent regeneration process is: when there is a certain pressure in the adsorption tower at the initial stage of regeneration, close the valves at both ends of the vacuum pump and open the valves on the second pipeline, and the desorbed oil and gas are transmitted through the second pipeline; when the pressure in the adsorption tower is reduced to normal pressure, close the valve on the second pipeline, open the valves at both ends of the vacuum pump for vacuum desorption. Although the patent proposes a process idea that pressurized absorption and adsorption is beneficial to reducing the size of the adsorption equipment and the amount of adsorbent used, there are many obvious defects or omissions in the key absorption and adsorption process flow and equipment, absorption and adsorption operating conditions, and the operating steps and control schemes of the adsorption part: First, the first adsorption zone of the adsorption tank is filled with molecular sieves, and oil and gas often contain a certain amount of water, which can easily cause the molecular sieve to deactivate; secondly, the process flow and operating steps of the adsorption part lack the key vacuum cleaning step, and the oil and gas recovery industry practice has proved that the vacuum cleaning step is indispensable for the oil and gas recovery process to achieve the "mg-level standard" of tail gas concentration; secondly, the process flow and operating steps of the adsorption part lack the key reverse charging step, and it is also difficult to obtain the "mg-level standard" " tail gas; secondly, in terms of process flow and operation steps, the necessary flow control means are lacking in the pressure reduction stage from adsorption pressure to normal pressure, and the vacuuming stage from normal pressure to vacuum. Thus, a large instantaneous amount of desorbed gas will circulate back to the compressor inlet line at the beginning of the pressure reduction process, thereby greatly increasing the load of the compressor; and the patent does not give a specific solution for more than two adsorption beds when the processing volume is large; and the device adopts a liquid ring compressor, and the absorption and adsorption pressure conditions are 0.2-0.3MPa, which has problems such as low absorption and adsorption pressure and low compressor efficiency; thirdly, in the hot summer season, the ambient temperature and the absorption oil temperature are both high, and the adsorption of high-concentration oil and gas releases heat, which makes it difficult to meet the technical requirements of relevant national standards, so the adsorption bed may have safety hazards. It is precisely because of the above-mentioned many defects and deficiencies that, although the patent has been applied for nearly ten years, there has been no report of successful application in the field of oil and gas recovery. Summary of the invention

[0006] In order to solve the above problems in the prior art, the present invention provides a pressurized absorption and adsorption oil and gas recovery process, which can stably achieve the mg-level standard for the concentration of total non-methane hydrocarbons in the tail gas.

[0007] To achieve the above object, the present invention provides the following technical solutions:

[0008] The present invention provides a process for recovering oil and gas by pressurized absorption and adsorption, wherein the main equipment used in the process for recovering oil and gas comprises at least: a compressor, an absorption tower, a vacuum pump, one of a lean oil pump or a rich oil pump, and an adsorption bed group, wherein the adsorption bed group comprises at least one adsorption bed in a simultaneous adsorption step, and at least one adsorption bed in a different regeneration step;

[0009] The oil and gas recovery process comprises: the raw oil and gas is pressurized by a compressor and enters an absorption tower, and is absorbed by absorption oil, and organic matter in the raw oil and gas is absorbed into the absorption oil, and flows out of the device with the rich absorption oil, and the non-condensable gas at the top of the tower enters the adsorption bed in the adsorption step of the adsorption bed group at an adsorption feed temperature of 0 to 50° C. for adsorption separation, and each adsorption bed in the adsorption bed group undergoes the following steps in sequence:

[0010] Adsorption step: the non-condensable gas at the top of the tower enters the adsorption bed from the inlet side of the adsorption bed under the absorption adsorption pressure. In the process of passing through the adsorption bed, the organic matter in the non-condensable gas is adsorbed by the adsorbent, and the qualified tail gas is discharged from the outlet side of the adsorption bed, and is directly discharged into the atmosphere after being reduced to atmospheric pressure by a pressure control valve;

[0011] When the adsorption bed reaches a certain adsorption saturation, the operation is switched and the adsorption bed is subjected to a regeneration operation including at least the following steps in sequence:

[0012] (1) Inversion step: the desorbed gas is discharged from the inlet side of the adsorption bed, and the pressure of the adsorption bed is gradually reduced to atmospheric pressure. The desorbed gas discharged during the inversion process is sent to the inlet of the compressor under the control of the regulating valve to mix with the feed gas;

[0013] (2) Vacuuming step: The adsorption bed is evacuated by a vacuum pump, and the adsorption bed is gradually evacuated to the vacuum pressure. During this process, the organic matter adsorbed on the adsorbent is desorbed, and the desorbed gas is pressurized by the vacuum pump and sent to the compressor inlet to mix with the feed gas;

[0014] (3) Vacuum cleaning step: while the adsorption bed is continuously evacuated by the vacuum pump, a cleaning gas is introduced from the outlet side of the adsorption bed to perform vacuum cleaning on the adsorption bed, thereby further desorbing the organic matter adsorbed on the adsorption bed and completely regenerating the adsorbent. The desorbed gas obtained during the vacuum cleaning process is pressurized by the vacuum pump and then sent to the compressor inlet to mix with the feed gas;

[0015] (4) Reverse charging step: introducing tail gas from the outlet side of the adsorption bed, and under the control of the regulating valve, reversely charging the adsorption bed to the absorption adsorption pressure;

[0016] Cycling the adsorption step and the regeneration operation steps (1) to (4) of the adsorption bed;

[0017] Under the control of computer logic, each adsorption bed in the adsorption bed group operates in sequence and staggeredly, forming a continuous adsorption process.

[0018] Preferably, the non-condensable gas at the top of the tower enters the adsorption bed group for adsorption separation at an adsorption feed temperature of 0 to 50° C., specifically:

[0019] If the hot spot temperature of the adsorption bed is not higher than the temperature limit of 60°C specified in the oil and gas recovery design specification, the adsorption feed temperature used is room temperature of 25-50°C, and the non-condensable gas at the top of the tower directly enters the adsorption bed group;

[0020] If the absorption process adopts the adsorption feed temperature of 25-50°C, but due to the high ambient temperature or absorption oil temperature, and the high Reid vapor pressure of light oil or absorption oil, which causes the hot spot temperature of the adsorption bed to be higher than the temperature limit of 60°C specified in the oil and gas recovery design specifications, a shallow cooler is installed on the non-condensable gas line at the top of the absorption tower to reduce the adsorption feed temperature to a shallow low temperature of 0-25°C, and the liquid condensed in the shallow cooling process is returned to the rich absorption oil at the bottom of the absorption tower.

[0021] The reason why the adsorption feed temperature is lowered to a low temperature of 0 to 25°C is that the adsorption process is an exothermic process, so the area where adsorption occurs in the adsorption bed will produce an adsorption temperature rise. The magnitude of the adsorption temperature rise is related to factors such as oil and gas concentration, oil and gas type, and adsorption capacity of the adsorbent. By lowering the adsorption feed temperature, the base temperature of the adsorption bed can be effectively lowered, thereby ensuring that the hot spot temperature of the adsorption bed will not exceed the temperature limit specified in the specification at any time.

[0022] Preferably, when the absorption oil is a light oil product other than crude oil, the absorption process of the absorption tower directly adopts shallow low temperature absorption of 0 to 25°C. That is, the lean absorption oil is cooled to a shallow low temperature of 0 to 25°C, and then the shallow low temperature absorption oil enters the absorption tower for absorption. Shallow low temperature absorption can not only reduce the temperature of the non-condensable gas at the top of the tower entering the adsorption bed, but also increase the absorption efficiency.

[0023] Preferably, the vacuum pressure in steps (2) and (3) of the regeneration operation of the adsorption bed is 1 to 20 kPa expressed as an absolute pressure.

[0024] Preferably, the cleaning gas in step (3) of the regeneration operation of the adsorption bed is a gas with a low organic concentration or containing no organic matter, including tail gas, external nitrogen, external air or vent gas.

[0025] Preferably, the inversion step in step (1) of the regeneration operation of the adsorption bed is specifically:

[0026] 1) Set up an inverted buffer tank, first connect the adsorption bed with the inverted buffer tank, achieve equal pressure in the two containers, and transfer part of the inverted desorption gas to the inverted buffer tank;

[0027] 2) the reverse desorption gas is then depressurized and released to the compressor inlet to mix with the feed gas until the adsorption bed is depressurized to atmospheric pressure;

[0028] 3) In other steps except step 2), when the desorbed gas is at a lower instantaneous flow rate, the desorbed gas in the inversion buffer tank is gradually discharged to the compressor inlet to mix with the raw gas until the pressure of the inversion buffer tank drops to atmospheric pressure.

[0029] The advantage of arranging the reverse step of the present invention in this way is that, in the early stage of the reverse step, the inlet side of the adsorption bed is first connected to the reverse buffer tank to quickly achieve pressure equalization. If the adsorption bed and the reverse buffer tank are of equal volume, about 50% of the reverse venting volume can be transferred to the reverse buffer tank; then, the reverse step 2) is continued from the pressure after pressure equalization, so that the average flow rate of the reverse venting is greatly reduced, thereby effectively reducing the load of the compressor; and after the reverse step 2) is completed, the total desorbed gas is in the other step stage of low instantaneous flow rate, and then the desorbed gas in the reverse buffer tank is gradually released to the compressor inlet to mix with the raw gas. This process arrangement can reduce the maximum reverse venting flow rate by about 50%, or even lower, thereby effectively reducing the maximum load of the compressor.

[0030] Preferably, a forward discharge step is provided before the reverse discharge step in step (1) of the regeneration operation of the adsorption bed. The specific process of the forward discharge step is: discharging the forward discharge gas from the outlet side of the adsorption bed into the atmosphere, or providing a forward discharge buffer tank to discharge the forward discharge gas into the forward discharge buffer tank that provides cleaning gas for the vacuum cleaning step.

[0031] The reason why the present invention sets a forward release step between the reverse release step and the adsorption step is that the forward release gas discharged in the forward release step is directly discharged into the atmosphere or used as a cleaning gas, and does not need to be circulated back to the compressor inlet. Therefore, the internal circulation volume can be reduced, which is beneficial to reducing the load of the entire device. However, the forward release step must be based on the premise of ensuring that the concentration of the discharged forward release gas does not exceed the standard.

[0032] Preferably, the absorption adsorption pressure is 300-1300 kPa expressed as absolute pressure.

[0033] More preferably, the absorption adsorption pressure is 600-900 kPa expressed as absolute pressure.

[0034] Preferably, the adsorbent includes activated carbon, silica gel, activated alumina, resin, or a layered filling of one or more of the above adsorbents.

[0035] The adsorption bed group described in the present invention includes at least one adsorption bed in a simultaneous adsorption step, which means that when the oil and gas processing scale of the device is large, two or more adsorption beds in a simultaneous adsorption step that are logically connected in parallel are arranged, and this adsorption bed operation mode can meet the requirements for adsorption space velocity when processing oil and gas of any scale; and at least one adsorption bed in a different regeneration step, which means that when the oil and gas processing volume is large and the regeneration load is large, two or more adsorption beds in different regeneration steps are arranged, among which at least one adsorption bed is always in a vacuuming or vacuum cleaning step, and the other adsorption bed is in other regeneration steps. The advantages of such an adsorption bed arrangement are: 1. The vacuum pump can be in an effective operating state throughout the whole process, so the vacuum regeneration efficiency of the device will be significantly improved, thereby reducing the investment and energy consumption of the device; 2. There is sufficient time to allow the reverse step to slowly and evenly reduce the pressure and release, without significantly increasing the instantaneous flow rate of the desorbed gas circulating back to the compressor due to rapid release; 3. Since the total desorption gas flow rate is the sum of the desorption gas flow rates from two or more different adsorption beds in different regeneration stages, there is sufficient condition to make the instantaneous flow rate of the desorption gas more uniform, thereby effectively reducing the maximum instantaneous load of the compressor.

[0036] Since the absorption process of the process of the present invention is carried out at a relatively high absorption pressure, the lean oil pump used to pressurize the lean absorption oil or the rich oil pump used to pressurize the rich absorption oil and send it out of the device can be selected according to the on-site conditions. That is, when the source pressure of the lean absorption oil is lower than the absorption pressure, the main equipment of the process of the present invention includes the lean oil pump. At this time, the lean absorption oil is pressurized to the absorption pressure by the lean oil pump and then sent to the absorption tower, and the rich absorption oil is regulated by the liquid level control loop and discharged from the device by self-pressure; and when the source pressure of the lean absorption oil is higher than the absorption pressure, the main equipment of the process of the present invention includes the rich oil pump. At this time, the lean absorption oil enters the absorption tower by self-pressure, and the rich absorption oil is regulated by the liquid level control loop and flows out of the device to the absorption oil source after being pressurized by the rich oil pump.

[0037] The compressor mentioned in the present invention is a device used to increase the pressure of the raw gas and the desorbed gas. Depending on the situation, a screw compressor, a liquid ring compressor, a centrifugal compressor, a reciprocating compressor, etc. can be selected. When the compression is relatively large, liquid spraying, cooling, liquid separation, etc. are often required. These are all conventional practices in this professional field and will not be described in detail here.

[0038] Compared with the prior art, the present invention has the following beneficial effects:

[0039] The present invention increases the pressure of oil and gas to a higher absorption pressure and then absorbs it. The single-pass recovery rate of the absorption part can reach about 90%, which also means that after the absorption treatment, the concentration and amount of organic matter entering the adsorption part are greatly reduced; and in the adsorption under pressure, the volume flow rate of the raw gas entering the adsorption bed is only a fraction of that under normal pressure, so not only the volume of the adsorption bed can be greatly reduced, but also the regeneration load can be greatly reduced, thereby greatly reducing the investment and operating energy consumption of the adsorption part; and through the reasonable setting of the adsorbent, process flow, equipment, timing steps and operating conditions of the adsorption part of the present invention, the process of the present invention is easier to obtain tail gas with extremely low non-methane total hydrocarbon concentration than the normal pressure adsorption process, for example, the non-methane total hydrocarbon concentration can reach <60mg / m 3 , and high organic matter recovery rate, such as the organic matter recovery rate can be as high as 99.95% or more; and the application research of the present invention shows that the higher the concentration of raw oil and gas, the higher the concentration of light components in the oil and gas, and the larger the scale of oil and gas processed, the more obvious the advantages of the process of the present invention. And the present invention is also applicable to the recovery of oil and gas with similar concentration and composition produced by other processes. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] The drawings constituting a part of the present application are used to provide a further understanding of the present application. The illustrative embodiments and descriptions of the present application are used to explain the present application and do not constitute an improper limitation on the present application. In the drawings:

[0041] Figure 1 This is a schematic flow diagram of a pressurized absorption and adsorption oil and gas recovery process according to Example 1 of the present invention, which uses two adsorption beds, shallow low-temperature absorption, an inverted buffer tank, and uses tail gas as cleaning gas;

[0042] Figure 2 This is a schematic flow chart of a pressurized absorption and adsorption oil and gas recovery process described in Example 2 of the present invention, which uses four adsorption beds, shallow low-temperature cooling of non-condensable gas at the top of the tower, a forward discharge step, a reverse discharge buffer tank, and uses air as a cleaning gas.

[0043] Figure numerals: 1, compressor; 2, absorption tower; 3, packing section; 4, lean oil pump; 5, shallow cooler 1; 6, vacuum pump; 7, reverse buffer tank; 8, shallow cooler 2; 11, pipeline 1; 12, pipeline 2; 13, pipeline 3; 14, pipeline 4; 15, pipeline 5; 16, pipeline 6; 17, pipeline 7; 18, regulating valve 1; 19, concentration monitor; 20, flame arrester; 21, pipeline 8; 22, regulating valve 2; 23, valve 1; 24, pipeline 9; 25, pipeline 13; 26, valve 2; 27, pipeline 10; 28, regulating valve 3; 29, valve 3; 30, pipeline 11; 31, valve 4; 32, pipeline 12;

[0044] A1, adsorption inlet valve of bed A; A2, vacuum valve of bed A; A3, reverse valve of bed A; A4, adsorption outlet valve of bed A; A5, reverse charging valve of bed A; A6, forward cleaning valve of bed A;

[0045] The A bed, B bed, C bed and D bed described in the figure are all adsorption beds. DETAILED DESCRIPTION

[0046] Now, various exemplary embodiments of the present invention are described in detail, and this detailed description should not be considered as a limitation of the present invention, but should be understood as a more detailed description of certain aspects, characteristics and embodiments of the present invention. It should be understood that the terms described in the present invention are only for describing specific embodiments and are not used to limit the present invention.

[0047] In addition, for the numerical range in the present invention, it is understood that each intermediate value between the upper and lower limits of the range is also specifically disclosed. Each smaller range between the intermediate value in any stated value or stated range and any other stated value or intermediate value in the range is also included in the present invention. The upper and lower limits of these smaller ranges can be independently included or excluded in the scope.

[0048] Unless otherwise stated, all technical and scientific terms used in this application have the same meanings as those of ordinary skill in the art described in the present invention. Although the present invention only describes preferred methods and materials, any methods and materials similar or equivalent to those described in this application may also be used in the implementation or testing of the present invention. All documents mentioned in this specification are incorporated by reference to disclose and describe the methods and / or materials related to the documents. In the event of a conflict with any incorporated document, the content of this specification shall prevail.

[0049] It will be apparent to those skilled in the art that various modifications and variations may be made to the specific embodiments of the present invention description without departing from the scope or spirit of the present invention. Other embodiments derived from the present invention description will be apparent to the skilled artisan. The present invention description and examples are exemplary only.

[0050] The words “include,” “including,” “have,” “contain,” etc. used in this application are open-ended terms, meaning including but not limited to.

[0051] The room temperature absorption described in the following embodiments of the present invention refers to the absorption temperature at the ambient temperature and the temperature of the absorption oil entering the device, that is, usually refers to 25-50°C.

[0052] Example 1

[0053] A pressurized absorption and adsorption oil and gas recovery process, the process flow chart is as follows Figure 1As shown, the main equipment includes a compressor (1), an absorption tower (2) with a packing section (3) inside, a lean oil pump (4), a shallow cooler (5), a vacuum pump (6), an inverted buffer tank (7) and an adsorption bed group consisting of two adsorption beds, namely an adsorption bed (Bed A) and an adsorption bed (B Bed);

[0054] The relatively high concentration oil gas generated during the light oil loading process is introduced into the device from pipeline 1 (11), mixed with the desorbed gas circulated back from pipeline 11 (30), and then pressurized by compressor (1) before entering the absorption tower (2) from the bottom through pipeline 2 (12); the lean absorption oil entering the device from the external system through pipeline 3 (13) is pressurized by the lean oil pump (4) and then passes through the shallow cooler (5) (the cooling load is provided by the refrigeration unit, which is a conventional operation in the field; of course, a heat exchanger can also be set before the shallow cooler to first exchange heat between the lean absorption oil and the rich absorption oil, and then perform shallow cooling to achieve energy saving. The purpose of energy conservation is that this is also a conventional practice in the field and is not shown in the figure) and then cooled to a slightly low temperature and enters the absorption tower (2) from the top; after the absorption oil enters the absorption tower (2), it is evenly distributed and then flows from top to bottom through the packing section (3). During this process, it countercurrently contacts with the oil and gas flowing from bottom to top through the packing section (3), and the organic matter in the oil and gas is absorbed into the absorption oil. The rich absorption oil that absorbs the recovered organic matter falls to the bottom of the tower and is discharged through the pipeline five (15) by self-pressure; and the lower concentration of the tower top non-condensable gas in equilibrium with the lean absorption oil enters the adsorption bed group through the pipeline six (16).

[0055] The above-mentioned adsorption bed group is composed of two adsorption beds, namely, adsorption bed (Bed A) and adsorption bed (Bed), and the adsorption beds are filled with adsorbent. At any time, one of them is in the adsorption step, and the other is in a different regeneration operation step. The two adsorption beds switch operations with each other. The following takes the adsorption bed (Bed A) as an example to explain the operation process of each adsorption bed; wherein the adsorption bed (Bed A) is in the adsorption step, and the adsorption bed (Bed A) undergoes the following operation steps in sequence:

[0056] Adsorption step: the adsorption inlet valve (A1) (the valves without special instructions are all program-controlled valves) and the adsorption outlet valve (A4) of the adsorption bed (A bed) are opened, and the other valves of the adsorption bed (A bed) are closed (the valves without instructions to be opened are closed valves), and the non-condensable gas is introduced into the adsorption bed (A bed) from the inlet. During the process of the oil and gas passing through the adsorption bed (A bed), the organic components with strong adsorption force are adsorbed by the adsorbent, and the inert gas components that are not easily adsorbed pass through the adsorbent bed layer and flow out from the outlet side of the adsorption bed (A bed) along the pipeline seven (17) as the tail gas, and after being reduced in pressure by the regulating valve one (18), the tail gas concentration is detected and recorded by the concentration monitor (19), and finally discharged into the atmosphere through the flame arrester (20);

[0057] When the adsorption front of organic matter on the adsorption bed (Bed A) approaches the outlet of the adsorption bed (Bed A) and the adsorption bed (Bed A) reaches a certain adsorption saturation, the operation is switched and the adsorption bed (Bed A) switches to the regeneration operation; the regeneration operation of the adsorption bed (Bed A) consists of 4 steps, namely, the reverse step, the vacuum step, the vacuum cleaning step and the reverse charging step:

[0058] (1) Reversal step: The purpose of the reversal step is to discharge the desorbed gas from the inlet side of the adsorption bed (Bed A) and gradually reduce the pressure of the adsorption bed (Bed A) to atmospheric pressure. The desorbed gas discharged during the reversal process is uniformly sent to the inlet of the compressor (1) to mix with the feed gas. Specifically,

[0059] The first step is to open the inversion valve (A3) and valve 2 (26) of the adsorption bed (Bed A) at the inlet side, connect the adsorption bed (Bed A) with the inversion buffer tank (7), achieve equal pressure in the two containers, and transfer part of the inversion desorption gas to the inversion buffer tank (7) in a short time;

[0060] The second step is to continue to open the A bed reverse valve (A3), and under the control of the regulating valve three (28), the reverse desorbed gas is evenly released to the compressor (1) inlet line through the pipeline ten (27) and the pipeline eleven (30) to mix with the raw gas until the adsorption bed (A bed) is depressurized to atmospheric pressure;

[0061] The third step is to open valve two (26) when the desorbed gas is at a relatively low instantaneous flow rate in the steps other than the second inversion step, and gradually discharge the desorbed gas in the inversion buffer tank (7) to the inlet line of the compressor (1) and mix with the raw gas under the control of the regulating valve three (28) until the pressure of the inversion buffer tank (7) is reduced to atmospheric pressure.

[0062] (2) Vacuuming step: Open the vacuuming valve (A2) and valve 3 (29) on the inlet side of the adsorption bed (A bed), and use the vacuum pump (6) to evacuate the adsorption bed (A bed), so that the pressure of the adsorption bed (A bed) gradually decreases to the vacuuming pressure. In this process, the organic components adsorbed on the adsorbent are gradually desorbed, and the desorbed gas of concentrated organic matter obtained at the outlet of the vacuum pump (6) is discharged to the inlet line of the compressor (1) through the pipeline 11 (30) to mix with the raw material gas.

[0063] (3) Vacuum cleaning step: continue to open the vacuum valve (A2) of bed A, and simultaneously open the reverse charging valve (A5) and valve 1 (23) of bed A. The low-concentration tail gas is used as cleaning gas and passes through pipeline 8 (21), pipeline 9 (24) and reverse charging valve (A5) of bed A, and then enters the adsorption bed (bed A) from the outlet side. Under the dual effects of vacuuming to reduce the total pressure and inert gas to reduce the oil and gas partial pressure, the organic matter adsorbed on the adsorbent is further desorbed. The desorbed gas obtained in the vacuum cleaning process is also discharged to the inlet line of the compressor (1) through pipeline 11 (30) to mix with the raw gas. After the vacuum cleaning step, the adsorption bed (bed A) is completely regenerated, and the adsorption bed (bed A) enters the reverse charging step.

[0064] (4) Reverse charging step: Open the A bed reverse charging valve (A5) on the outlet side of the adsorption bed (A bed), and introduce tail gas under the control of the regulating valve 2 (22). The tail gas enters the adsorption bed (A bed) through the pipeline 8 (21), the regulating valve 2 (22) and the A bed reverse charging valve (A5), and evenly and gradually reverses the adsorption bed (A bed) to the absorption adsorption pressure.

[0065] At this point, an adsorption regeneration cycle of the adsorption bed (bed A) is completed, and then the cycle enters the next adsorption regeneration cycle.

[0066] The adsorption bed (B bed) is also operated in the same manner as the adsorption bed (A bed), except that the corresponding position valves on the inlet and outlet sides of the adsorption bed (A bed) are changed to the corresponding position valves on the inlet and outlet sides of the adsorption bed (B bed) (not marked in the figure), and the other operation processes are the same as those of the adsorption bed (A bed), which will not be repeated here. In this way, the two adsorption beds are switched alternately, and the entire process is operated under the logic control of the PLC according to the logic and timing steps set by the program, so as to realize the continuity of the entire adsorption regeneration process.

[0067] Example 2

[0068] A pressurized absorption and adsorption oil and gas recovery process, the process flow chart is as follows Figure 2 As shown, the main equipment includes a compressor (1), an absorption tower (2) with a packing section (3) inside, a lean oil pump (4), a shallow cooler (8), a vacuum pump (6), an inverted buffer tank (7) and an adsorption bed group consisting of four adsorption beds;

[0069] The relatively high concentration oil gas generated during the light oil loading process is introduced into the device through pipeline 1 (11), mixed with the desorbed gas circulated back through pipeline 11 (30), and then pressurized by the compressor (1) and enters the absorption tower (2) from the bottom through pipeline 2 (12); the lean absorption oil entering the device from the external system through pipeline 3 (13) is pressurized by the lean oil pump (4) and enters the absorption tower (2) from the top. After entering the absorption tower (2), the absorption oil is evenly distributed and then flows from top to bottom through the packing section (3), where it passes through the During the process, the gas and oil flow from bottom to top through the packing section (3) in countercurrent contact, and the organic matter in the gas and oil is absorbed into the absorption oil. The rich absorption oil that absorbs the recovered organic matter falls to the bottom of the tower and is discharged from the device through pipeline five (15) by self-pressure. The non-condensable gas at the top of the tower, which is in equilibrium with the lean absorption oil, is cooled to a shallow low temperature by shallow cooler two (8) and then enters the adsorption bed group through pipeline six (16). The condensate produced by shallow cooling enters the bottom of the absorption tower (2) through pipeline four (14) and pipeline two (12) and is mixed with the rich absorption oil.

[0070] The above-mentioned adsorption bed group is composed of four adsorption beds, namely, adsorption bed (A bed), adsorption bed (B bed), adsorption bed (C bed) and adsorption bed (D bed). The adsorption beds are filled with adsorbents. At any time, two of them are in the simultaneous adsorption step, and the other two are in different regeneration operation steps. The four adsorption beds are switched to operate each other. The following takes the adsorption bed (A bed) as an example to explain the operation process of each adsorption bed. The adsorption bed (A bed) undergoes the following operation steps in sequence:

[0071] Adsorption step: the adsorption inlet valve (A1) and the adsorption outlet valve (A4) of the adsorption bed (A bed) are opened, and non-condensable gas is introduced into the adsorption bed (A bed) from the inlet of the adsorption bed (A bed). When the oil and gas pass through the adsorption bed (A bed), the organic components with strong adsorption force are adsorbed by the adsorbent, and the inert gas components that are not easily adsorbed pass through the adsorbent bed layer and flow out from the outlet side of the adsorption bed (A bed) along the pipeline seven (17) as tail gas, and after being reduced in pressure by the regulating valve one (18), the tail gas concentration is detected and recorded by the concentration monitor (19), and finally discharged into the atmosphere through the flame arrester (20);

[0072] When the adsorption bed (Bed A) reaches a certain adsorption saturation, the operation is switched and the adsorption bed (Bed A) switches to the regeneration operation; the regeneration operation of the adsorption bed (Bed A) consists of 5 steps, which are the forward placement step, the reverse placement step, the vacuum step, the vacuum cleaning step and the reverse charging step:

[0073] (1) Discharge step: Open the discharge cleaning valve (A6) and valve 4 (31) on the outlet side of the adsorption bed (Bed A), and the discharge gas discharged from the outlet side of the adsorption bed (Bed A) is mixed with the tail gas along pipeline 12 (32), and then the concentration of the tail gas is detected and recorded by the concentration monitor (19), and finally discharged into the atmosphere through the flame arrester (20);

[0074] (2) Reversal step: The purpose of the reversal step is to discharge the desorbed gas from the inlet side of the adsorption bed (Bed A) and gradually reduce the pressure of the adsorption bed (Bed A) to atmospheric pressure. The desorbed gas discharged during the reversal process is uniformly sent to the inlet of the compressor (1) to mix with the feed gas. Specifically,

[0075] The first step is to open the inversion valve (A3) and valve 2 (26) of the adsorption bed (Bed A) at the inlet side, connect the adsorption bed (Bed A) with the inversion buffer tank (7), achieve equal pressure in the two containers, and transfer part of the inversion desorption gas to the inversion buffer tank (7) in a short time;

[0076] The second step is to continue opening the A bed reverse valve (A3), and under the control of the regulating valve three (28), the reverse desorbed gas is evenly released to the compressor (1) inlet line through the pipeline thirteen (25), the pipeline ten (27) and the pipeline eleven (30) to be mixed with the raw gas until the adsorption bed (A bed) is depressurized to atmospheric pressure;

[0077] The third step is that in the steps other than the second inversion step, when the desorbed gas is at a relatively low instantaneous flow rate, valve two (26) is opened, and under the control of regulating valve three (28), the desorbed gas in the inversion buffer tank (7) is gradually discharged along pipeline ten (27) and pipeline eleven (30) to the inlet line of the compressor (1) to be mixed with the raw gas until the pressure of the inversion buffer tank (7) is reduced to atmospheric pressure.

[0078] (3) Vacuuming step: Open the vacuuming valve (A2) on the inlet side of the adsorption bed (Bed A), and use the vacuum pump (6) to evacuate the adsorption bed (Bed A), so that the pressure of the adsorption bed (Bed A) is gradually reduced to the vacuuming pressure. In this process, the organic components adsorbed on the adsorbent are gradually desorbed, and the desorbed gas of concentrated organic matter obtained at the outlet of the vacuum pump (6) is discharged to the inlet line of the compressor (1) through the pipeline 11 (30) to mix with the raw material gas.

[0079] (4) Vacuum cleaning step: continue to open the A bed vacuum valve (A2), and at the same time open the A bed downstream cleaning valve (A6) and valve one (23). The low-concentration tail gas is used as cleaning gas through pipeline nine (24) and A bed downstream cleaning valve (A6), and then enters the adsorption bed (A bed) from the outlet side. Under the dual effects of vacuuming to reduce the total pressure and inert gas to reduce the oil and gas partial pressure, the organic matter adsorbed on the adsorbent is further desorbed. The desorbed gas obtained in the vacuum cleaning process is also discharged to the compressor (1) inlet line through pipeline eleven (30) to mix with the raw gas. After the vacuum cleaning step, the adsorption bed (A bed) is completely regenerated, and the adsorption bed (A bed) enters the reverse charging step.

[0080] (5) Reverse charging step: Open the reverse charging valve (A5) of bed A at the outlet side of the adsorption bed (bed A), and introduce tail gas under the control of regulating valve 2 (22). The tail gas enters the adsorption bed (bed A) through pipeline 8 (21), regulating valve 2 (22) and reverse charging valve (A5) of bed A, and evenly and gradually reversely charges the adsorption bed (bed A) to the absorption adsorption pressure.

[0081] At this point, an adsorption regeneration cycle of the adsorption bed (bed A) is completed, and then the cycle enters the next adsorption regeneration cycle.

[0082] Adsorption bed (B bed), adsorption bed (C bed) and adsorption bed (D bed) are also operated in the same manner as adsorption bed (A bed), except that the corresponding position valves on the inlet and outlet sides of the above-mentioned adsorption bed (A bed) are changed to the corresponding position valves on the inlet and outlet sides of adsorption bed (B bed), adsorption bed (C bed) and adsorption bed (D bed) (not marked in the figure), and the other operation processes are the same as those of adsorption bed (A bed), which will not be repeated here. In this way, the four adsorption beds are switched alternately, and the entire process is operated under the logic control of the PLC according to the logic and timing steps set by the program, so as to realize the continuity of the entire adsorption regeneration process.

[0083] Application Case 1:

[0084] The oil and gas flow rate of a train loading platform during gasoline loading is 1000m 3 / h, oil and gas concentration 35v%, the pressurized absorption and adsorption oil and gas recovery process of Example 1 is used for recovery treatment. The device adopts 2 adsorption beds, shallow low-temperature absorption, with an inverted buffer tank, and uses tail gas as a pressurized absorption and adsorption oil and gas recovery process for cleaning gas. The absorption tower is a packed tower structure. The adsorbents filled in the two adsorption beds are silica gel and activated carbon. The compressor adopts a screw compressor, the adsorption pressure is 800kPa (absolute), and the gasoline from the tank area is used as the absorption oil. The absorption oil volume is 35t / h, the absorption temperature is 10℃, and the rich absorption oil returns to the gasoline tank in the tank area. After absorption treatment, the concentration of non-condensable gas at the top of the tower drops to 4v%, and then enters the adsorption bed group. The adsorption bed group operates according to the timing steps shown in Table 1:

[0085] Table 1 Adsorption bed operation schedule

[0086]

[0087] Note: A—adsorption step; DP—reverse placement step; V—vacuuming step; VP—vacuum cleaning step; FR—reverse charging step.

[0088] Among them, the first step of the inversion step is to connect the adsorption bed with the inversion buffer tank and then pressurize them to 450kPa (absolute), the second step is to evenly reduce the pressure of the adsorption bed to about 100kPa (absolute) under the control of the regulating valve, and the third step is to gradually release the pressure of the inversion buffer tank to about 100kPa (absolute) under the control of the regulating valve during the low desorption gas flow rate periods of the 4th and 5th periods.

[0089] After the above-mentioned recovery process, the concentration of non-methane total hydrocarbons in the tail gas discharged by the device is less than 20mg / m 3 The total non-methane hydrocarbon recovery rate of the device is >99.99%, and the hot spot temperature of the device is <50℃.

[0090] Application Case 2:

[0091] The oil and gas flow rate of a terminal during the crude oil loading process is 10000m 3 / h, oil and gas concentration 33v%, the pressurized absorption and adsorption oil and gas recovery process of Example 2 is used for recovery and treatment. The device adopts 4 adsorption beds, shallow low-temperature cooling of the non-condensable gas at the top of the tower, with an inverted buffer tank, with a forward step, and a pressurized absorption and adsorption oil and gas recovery process using air as the cleaning gas. The absorption tower is a packed tower structure. The adsorbents filled in the 4 adsorption beds are silica gel and activated carbon. The compressor adopts a screw compressor, the adsorption pressure is 800kPa (absolute), and the crude oil introduced into the device from the loading line is used as the absorption oil. The pressure of the absorption oil entering the device is 400kPa (absolute), the absorption oil volume is 400t / h, the absorption temperature is room temperature, and the rich absorption oil is returned to the loading line by self-pressure. After the non-condensable gas at the top of the tower is shallowly cooled to 10°C, the concentration drops to 4.5v% and enters the adsorption bed group. The adsorption bed group operates according to the timing steps shown in Table 2:

[0092] Table 2 Adsorption bed operation schedule

[0093]

[0094] Note: A—adsorption step; PP—forward placement step; DP—reverse placement step; V—vacuuming step; VP—vacuum cleaning step; FR—reverse charging step.

[0095] Among them, the forward step reduces the pressure of the adsorption bed to 600 kPa (absolute); the first step of the reverse step connects the adsorption bed with the reverse buffer tank and then pressurizes them to 350 kPa (absolute); the second step uniformly reduces the pressure of the adsorption bed to about 100 kPa (absolute) under the control of the regulating valve; the third step, at the end of the 4th period and the low desorption gas flow rate period of the 5th period, gradually releases the pressure of the reverse buffer tank to about 100 kPa (absolute) under the control of the regulating valve.

[0096] After the above-mentioned recovery process, the concentration of total non-methane hydrocarbons in the tail gas discharged by the device is less than 50mg / m 3The total non-methane hydrocarbon recovery rate of the device is >99.95%, and the hot spot temperature of the device is <50℃.

[0097] The above description is only a preferred specific implementation manner of the present invention, and the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes according to the technical scheme and inventive concept of the present invention within the technical scope disclosed by the present invention, and they should be covered by the protection scope of the present invention.

Claims

1. A process for recovering oil and gas by pressurized absorption, characterized in that: The main equipment used in the oil and gas recovery process at least includes: a compressor, an absorption tower, a vacuum pump, one of a lean oil pump or a rich oil pump, and an adsorption bed group, wherein the adsorption bed group includes at least one adsorption bed in a simultaneous adsorption step and at least one adsorption bed in a different regeneration step; The oil and gas recovery process comprises: the raw oil and gas enters the absorption tower after being pressurized by the compressor, is absorbed by the absorption oil, and the organic matter in the raw oil and gas is absorbed into the absorption oil, and flows out of the device with the rich absorption oil, and the non-condensable gas at the top of the tower enters the adsorption bed in the adsorption step of the adsorption bed group at the adsorption feed temperature of 0 to 50° C. for adsorption separation, and each adsorption bed in the adsorption bed group undergoes the following steps in sequence: Adsorption step: the non-condensable gas at the top of the tower enters the adsorption bed from the inlet side of the adsorption bed under the absorption adsorption pressure. In the process of passing through the adsorption bed, the organic matter in the non-condensable gas is adsorbed by the adsorbent, and the qualified tail gas is discharged from the outlet side of the adsorption bed, and is directly discharged into the atmosphere after being reduced to atmospheric pressure by a pressure control valve; When the adsorption bed reaches a certain adsorption saturation, the operation is switched and the adsorption bed is subjected to a regeneration operation including at least the following steps in sequence: (1) Inversion step: the desorbed gas is discharged from the inlet side of the adsorption bed, and the pressure of the adsorption bed is gradually reduced to atmospheric pressure. The desorbed gas discharged during the inversion process is sent to the inlet of the compressor under the control of the regulating valve to mix with the feed gas; (2) Vacuuming step: The adsorption bed is evacuated by a vacuum pump, and the adsorption bed is gradually evacuated to the vacuum pressure. During this process, the organic matter adsorbed on the adsorbent is desorbed, and the desorbed gas is pressurized by the vacuum pump and sent to the compressor inlet to mix with the feed gas; (3) Vacuum cleaning step: while the adsorption bed is continuously evacuated by the vacuum pump, a cleaning gas is introduced from the outlet side of the adsorption bed to perform vacuum cleaning on the adsorption bed, thereby further desorbing the organic matter adsorbed on the adsorption bed and completely regenerating the adsorbent. The desorbed gas obtained during the vacuum cleaning process is pressurized by the vacuum pump and then sent to the compressor inlet to mix with the feed gas; (4) Reverse charging step: introducing tail gas from the outlet side of the adsorption bed, and under the control of the regulating valve, reversely charging the adsorption bed to the absorption adsorption pressure; Cycling the adsorption step and regeneration steps (1) to (4) of the adsorption bed; Under the control of computer logic, each adsorption bed in the adsorption bed group operates in sequence and staggeredly, forming a continuous adsorption process.

2. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The non-condensable gas at the top of the tower enters the adsorption bed group at an adsorption feed temperature of 0 to 50° C. for adsorption separation, specifically: If the hot spot temperature of the adsorption bed is not higher than the temperature limit of 60°C specified in the oil and gas recovery design specification, the adsorption feed temperature used is room temperature of 25 to 50°C, and the non-condensable gas at the top of the tower directly enters the adsorption bed group; If the absorption process adopts the adsorption feed temperature of 25-50°C, but due to the high ambient temperature or absorption oil temperature, and the high Reid vapor pressure of light oil or absorption oil, which causes the hot spot temperature of the adsorption bed to be higher than the temperature limit of 60°C specified in the oil and gas recovery design specifications, a shallow cooler is installed on the non-condensable gas line at the top of the absorption tower to reduce the adsorption feed temperature to a shallow low temperature of 0-25°C, and the liquid condensed in the shallow cooling process is returned to the rich absorption oil at the bottom of the absorption tower.

3. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: When the absorption oil is a light oil product other than crude oil, the absorption process of the absorption tower directly adopts shallow low-temperature absorption at 0 to 25°C.

4. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The vacuum pressure in steps (2) and (3) of the regeneration operation of the adsorption bed is 1 to 20 kPa in absolute pressure.

5. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The cleaning gas in step (3) of the regeneration operation of the adsorption bed is a gas with a low organic concentration or containing no organic matter, including tail gas, external nitrogen, external air or vent gas.

6. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The inversion step in step (1) of the regeneration operation of the adsorption bed is specifically as follows: 1) Set up an inverted buffer tank, first connect the adsorption bed with the inverted buffer tank, achieve equal pressure in the two containers, and transfer part of the inverted desorption gas to the inverted buffer tank; 2) the reverse desorption gas is then depressurized and released to the compressor inlet to mix with the feed gas until the adsorption bed is depressurized to atmospheric pressure; 3) In the steps other than step 2), when the desorbed gas is at a lower instantaneous flow rate, the desorbed gas in the inversion buffer tank is gradually discharged to the compressor inlet to mix with the raw gas until the pressure of the inversion buffer tank drops to atmospheric pressure.

7. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: A forward discharge step is provided before the reverse discharge step in step (1) of the regeneration operation of the adsorption bed. The specific process of the forward discharge step is: discharging the forward discharge gas from the outlet side of the adsorption bed into the atmosphere, or providing a forward discharge buffer tank to discharge the forward discharge gas into the forward discharge buffer tank that provides cleaning gas for the vacuum cleaning step.

8. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: When the oil and gas processing scale of the device is large, two or more adsorption beds which are logically connected in parallel and are in the simultaneous adsorption step are set up; when the oil and gas processing volume is large and the regeneration load is also large, two or more adsorption beds which are in different regeneration steps are set up, among which at least one adsorption bed is always in the vacuuming or vacuum cleaning step, and the other adsorption bed is in other regeneration steps.

9. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The absorption pressure is expressed as 300 to 1300 kPa in absolute pressure.

10. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1 or 9, characterized in that: The absorption adsorption pressure is expressed as 600 to 900 kPa in absolute pressure.

11. The process for recovering oil and gas by pressurized absorption and adsorption according to claim 1, characterized in that: The adsorbent includes activated carbon, silica gel, activated alumina, resin, or a layered filling of one or more of the above adsorbents.

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