CN118045388A - Gas injection oil reservoir low-hydrocarbon tail gas full-separation recovery method and system - Google Patents
Gas injection oil reservoir low-hydrocarbon tail gas full-separation recovery method and system Download PDFInfo
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- 238000011084 recovery Methods 0.000 title claims abstract description 45
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000002347 injection Methods 0.000 title claims abstract description 32
- 239000007924 injection Substances 0.000 title claims abstract description 32
- 238000000926 separation method Methods 0.000 title claims description 58
- 239000007789 gas Substances 0.000 claims abstract description 198
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 113
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 90
- 238000001179 sorption measurement Methods 0.000 claims abstract description 86
- 239000003463 adsorbent Substances 0.000 claims abstract description 54
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 39
- 239000002250 absorbent Substances 0.000 claims abstract description 34
- 230000002745 absorbent Effects 0.000 claims abstract description 34
- 230000008929 regeneration Effects 0.000 claims abstract description 33
- 238000011069 regeneration method Methods 0.000 claims abstract description 33
- 238000007906 compression Methods 0.000 claims abstract description 26
- 230000006835 compression Effects 0.000 claims abstract description 26
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 24
- 238000005261 decarburization Methods 0.000 claims abstract description 23
- 238000004064 recycling Methods 0.000 claims abstract description 10
- 238000009833 condensation Methods 0.000 claims abstract description 9
- 230000005494 condensation Effects 0.000 claims abstract description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 33
- 150000002430 hydrocarbons Chemical class 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 238000004458 analytical method Methods 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 15
- 230000001172 regenerating effect Effects 0.000 claims description 15
- 229920006395 saturated elastomer Polymers 0.000 claims description 10
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- 239000011261 inert gas Substances 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 238000005262 decarbonization Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 2
- 239000003921 oil Substances 0.000 abstract description 25
- 239000010779 crude oil Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 abstract description 3
- 230000008569 process Effects 0.000 abstract description 3
- 238000005728 strengthening Methods 0.000 abstract description 3
- 239000005431 greenhouse gas Substances 0.000 abstract description 2
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- 238000005516 engineering process Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
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- 239000003345 natural gas Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
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- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
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- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
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- 239000001257 hydrogen Substances 0.000 description 1
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- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention belongs to the field of waste gas treatment and greenhouse gas control and utilization, and discloses a method and a system for fully separating and recovering low-hydrocarbon tail gas of a gas injection oil reservoir, wherein the method comprises the following steps: compressing and condensing the tail gas; decarburizing the tail gas after compression and condensation by using a special absorbent for carbon dioxide; performing primary pressure swing adsorption on the tail gas after decarburization treatment by using a primary adsorbent; and carrying out secondary variable pressure adsorption on the tail gas after primary variable pressure adsorption by using a secondary adsorbent. The invention ensures that crude oil associated gas is completely recycled by adopting the comprehensive gas recycling process of compression condensation, decarburization, primary pressure swing adsorption, secondary pressure swing adsorption, strengthening regeneration and recovery of pressure energy of tail gas with pressure, has low energy consumption and economic value, can separate other gases such as nitrogen and carbon dioxide, and has higher gas purity, methane purity of more than 90%, nitrogen purity of more than 99% and carbon dioxide purity of more than 99%.
Description
Technical Field
The invention belongs to the field of waste gas treatment and greenhouse gas control and utilization, and particularly relates to a method and a system for fully separating and recycling low-hydrocarbon tail gas of a gas injection oil reservoir.
Background
The low hydrocarbon tail gas is mainly generated in oil and gas fields developed by gas injection, such as air injection, oxygen reduction air, nitrogen, carbon dioxide and the like, the most difficult to treat is the tail gas generated by the air injection or oxygen reduction air technology, the gas is subjected to low-temperature, medium-temperature or high-temperature oxidation reaction with crude oil underground, and when O 2 in the air is consumed, the flue gas formed by mixing N 2 and other gases is discharged together through a production well to form the tail gas. The tail gas has complex components and mainly comprises a plurality of gases such as hydrocarbon, N 2, carbon dioxide, CO and the like. In the air injection development of the thin oil reservoir and the condensate oil reservoir, the hydrocarbon content is 10% -15%, mainly methane and other hydrocarbons, including a small part of heavy hydrocarbon, and other gases are about 85% -90%.
In the aspect of site safety, the lower explosion limit of light hydrocarbon is lower, for example, the lower explosion limit of methane is 5 percent, and ethane is 3 percent. Therefore, the injected air exhaust gas cannot be directly discharged into the air, and the air must be treated before being discharged. In recycling, the tail gas contains light hydrocarbon and a small part of heavy hydrocarbon due to lower hydrocarbon content, and the molecular particle size of methane and nitrogen (methaneNitrogen gas) The differences are very small, the polarities are very close, the separation difficulty is high, a plurality of separation technologies are needed to be combined, and no separation technology is applied in the petroleum industry at present.
At present, the following gas separation methods are mainly adopted:
1. Solution absorption method: the purpose of gas separation is achieved through dissolution or chemical reaction absorption of certain components in the raw material gas by the solution; the catalyst is widely and successfully used for acid gas extraction, such as carbon dioxide extraction, hydrogen sulfide extraction and the like of natural gas of synthesis gas. There are also methods for purifying methane from methane hydrate (combustible ice) principle, i.e. methane in gas reacts with water to produce combustible ice, thereby separating methane in gas. However, because the synthesis of combustible ice requires higher methane partial pressure and specific temperature, the synthesis speed is extremely slow, and the distance can be industrially utilized in a large gap at present, the method is not suitable for the separation effect of gas and the investment operation cost.
2. Membrane separation method: under a certain pressure, the molecular diameters and polarity of different components in the raw material gas are utilized to separate under the different penetrability of the polymer fiber membrane, such as permeation separation and purification of hydrogen gas (with small molecular diameter) and oil gas (separation between inorganic and organic molecules and utilizing the solubility of the organic molecules) from the mixed gas under a higher pressure, and the molecular diameters of methane and nitrogen (respectively) And polarity are very similar, from the current research results: the difficulty of separating and purifying methane by using the membrane is high, and only the MTR company in the United states has a methane and nitrogen separation membrane, but the separation efficiency is low and the application range is limited.
3. Cryogenic separation process: aiming at different standard boiling points of different components in raw material gas, certain components in mixed gas are liquefied preferentially at low temperature in a deep cooling mode, then gas-liquid separation or rectification is carried out to achieve the purpose of separation, and investment and operation energy consumption of the deep cooling separation are closely related to partial pressure and content of methane. However, the defects of the cryogenic technology are obvious, the device is complex, the equipment investment is large, the energy consumption is high, and the concentrations of CH 4 in the coal bed gas, the natural gas, the methane and the oilfield gas are not very high, so that the cryogenic separation technology is obviously unsuitable for the efficient separation of low-quality methane gas, but is more suitable for the separation of heavy hydrocarbon components.
4. Pressure swing adsorption process: the method is used for gas separation and purification, and is the best method for gas separation which is currently accepted because of lower investment, high automation degree and low operation cost. The separation and purification principle of the method is as follows: the gas separation method is characterized in that the difference of the diameters and the polarities of gas molecules of different components is large, and the gas separation method is carried out by utilizing the difference of the adsorption capacities of the special adsorption materials for the gases with different diameters and polarities. The adsorption material can be smoothly desorbed to achieve regeneration under the condition of reduced pressure, so that the special adsorption material can be recycled. The Pressure Swing Adsorption (PSA) process technology is mature, thousands of sets of PSA devices for separating and purifying hydrogen, oxygen, nitrogen, carbon dioxide, carbon monoxide and other conventional gases from mixed gases are newly built worldwide every year, and the PSA device can be suitable for separating methane and nitrogen.
Because the recovery technology of low-hydrocarbon tail gas in the oil field has not been put into practical application at present and the research and development of separation flow design for the tail gas has not been specially carried out, it is necessary to provide a gas injection oil reservoir low-hydrocarbon tail gas full-separation recovery method.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a full separation recovery method of low hydrocarbon tail gas of a gas injection oil reservoir, which ensures complete recycling of crude oil associated gas through a comprehensive gas utilization recovery process of compression, condensation, decarburization, primary pressure swing adsorption, secondary pressure swing adsorption, strengthening a regeneration system and recovery of tail gas pressure energy with pressure.
In order to achieve the above purpose, the present invention provides the following technical solutions:
a gas injection oil reservoir low hydrocarbon tail gas full separation recovery method comprises the following steps:
Compressing and condensing the tail gas;
Decarburizing the tail gas after compression and condensation by using a special absorbent for carbon dioxide;
Performing primary pressure swing adsorption on the tail gas after decarburization treatment by using a primary adsorbent;
and carrying out secondary pressure swing adsorption on the tail gas subjected to the primary pressure swing adsorption by using a secondary adsorbent to obtain nitrogen.
Further, the tail gas is compressed and condensed, which comprises:
Compressing the tail gas under normal pressure to 0.8-1.2 MPa;
and cooling the compressed tail gas to 0 ℃ to obtain a first condensate.
Further, after compression condensing the tail gas, it includes:
and (3) oil-water separation is carried out on the first condensate liquid to obtain first condensate oil.
Further, after decarbonizing the compressed and condensed tail gas by using a carbon dioxide special absorbent, the method comprises the following steps:
And removing and recovering the carbon dioxide in the absorbent special for saturated carbon dioxide.
Further, after the decarburization-treated tail gas is subjected to the primary pressure swing adsorption by the primary adsorbent, the method comprises the steps of:
Condensing and regenerating the saturated primary adsorbent to obtain a second condensate;
and (3) carrying out oil-water separation on the second condensate liquid to obtain second condensate oil.
Further, the primary adsorbent is a combined adsorption packing for separating high boiling point substances.
Further, after the tail gas after the primary pressure swing adsorption is subjected to the secondary pressure swing adsorption by using the secondary adsorbent, the method comprises the following steps:
The residual pressure recycling is carried out on the nitrogen obtained after the secondary variable pressure adsorption;
Regenerating the saturated secondary adsorbent to obtain methane;
Methane was concentrated to 90% under pressure.
Further, the secondary adsorbent is a methane-specific adsorbent.
On the other hand, the invention discloses a low-hydrocarbon tail gas full-separation recovery system of a gas injection oil reservoir, which comprises a compression condensing device, a decarburization treatment device, a primary pressure swing adsorption device and a secondary pressure swing adsorption device;
The compression condensing device is used for compressing and condensing the tail gas, and a gas outlet of the compression condensing device is connected with a gas inlet of the decarburization treatment device;
the decarbonization device is used for decarbonizing the compressed and condensed tail gas by matching with a special absorbent for carbon dioxide, and a gas outlet of the decarbonizing device is connected with a gas inlet of the primary pressure swing adsorption device;
The primary pressure swing adsorption device is used for carrying out primary pressure swing adsorption on the tail gas after decarburization treatment by matching with the primary adsorbent, and a gas outlet of the primary pressure swing adsorption device is connected with a gas inlet of the secondary pressure swing adsorption device;
The secondary pressure-variable adsorption device is used for carrying out secondary pressure-variable adsorption on the tail gas after primary pressure-variable adsorption by matching with the secondary adsorbent to obtain nitrogen.
Further, a liquid outlet of the compression condensing device is connected with an inlet of a condensate recovery device, and the condensate recovery device is used for collecting first condensate generated by compression condensing tail gas;
The outlet of the condensate recovery device is connected with the inlet of the oil-water separation device, and the oil-water separation device is used for separating condensate oil and water in the condensate;
The condensate outlet of the oil-water separation device is connected with the inlet of a condensate storage tank, and the condensate storage tank is used for storing condensate.
Further, an absorbent outlet of the decarburization treatment device is connected with an inlet of an absorbent regeneration device, and the absorbent regeneration device is used for regenerating the absorbent special for saturated carbon dioxide and removing carbon dioxide in the absorbent special for saturated carbon dioxide;
the gas outlet of the absorbent regeneration device is connected with the inlet of the carbon dioxide recovery device, and the carbon dioxide recovery device is used for recovering the carbon dioxide removed by the absorbent special for saturated carbon dioxide.
Further, an adsorbent outlet of the primary pressure swing adsorption device is connected with an inlet of the primary vacuum analysis device, a liquid outlet of the primary vacuum analysis device is connected with an inlet of the oil-water separation device, and the primary vacuum analysis device is used for analyzing and regenerating the saturated primary adsorbent to obtain second condensate;
the adsorbent outlet of the secondary variable pressure adsorption device is connected with the inlet of the secondary vacuum analysis device, and the secondary vacuum analysis device is used for analyzing and regenerating the saturated secondary adsorbent and removing methane.
Further, a gas outlet of the secondary variable pressure adsorption device is connected with a gas inlet of a methane concentration device, and the methane concentration device is used for pressurizing and concentrating methane to 90 percent concentration;
The outlet of the methane concentration device is connected with the inlet of the methane recovery device, and the methane recovery device is used for recovering, storing and pressurizing and concentrating methane.
Further, the adsorbent outlets of the primary vacuum analysis device and the secondary vacuum analysis device are connected with the inlet of the enhanced regeneration device, and the enhanced regeneration device is used for carrying out further regeneration treatment on the primary adsorbent and the secondary adsorbent in a mode of combining a plurality of regeneration modes by matching with inert gas.
Further, the liquid outlet of the enhanced regeneration device is connected with the inlet of the oil-water separation device.
The invention has the technical effects and advantages that:
the invention ensures the complete recycling of crude oil associated gas by adopting the comprehensive gas utilization and recovery process of compression condensation, decarburization, primary pressure swing adsorption, secondary pressure swing adsorption, strengthening regeneration and recovery of tail gas pressure energy with pressure, and has low energy consumption and economic value; by optimizing the recovery flow of each component in the tail gas, the low-concentration high-value light hydrocarbon and methane in the tail gas can be recovered, and other gases such as nitrogen and carbon dioxide can be separated, and the gas purity is higher, the methane purity is higher than 90%, the nitrogen purity is higher than 99%, and the carbon dioxide purity is higher than 99%; by adopting a high-strength regeneration mode under the protection of nitrogen, the regeneration efficiency and the service life of the adsorption material are ensured, the adsorption equipment is ensured to be in an inert gas protection state during regeneration, fire hazards are avoided, and the regenerated bed layer is ensured to be in a low-temperature and dry favorable environment.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention may be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.
Drawings
FIG. 1 is a flow chart of a method for fully separating and recovering low hydrocarbon tail gas of a gas injection oil reservoir;
FIG. 2 is a schematic diagram of a system for fully separating and recovering low hydrocarbon tail gas of a gas injection reservoir according to the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
FIG. 1 is a flow chart of a method for fully separating and recovering low hydrocarbon tail gas of a gas injection oil reservoir, and as shown in FIG. 1, the invention provides a method for fully separating and recovering low hydrocarbon tail gas of a gas injection oil reservoir, which comprises the following steps:
Compressing and condensing the tail gas;
Decarburizing the tail gas after compression and condensation by using a special absorbent for carbon dioxide;
Performing primary pressure swing adsorption on the tail gas after decarburization treatment by using a primary adsorbent;
and carrying out secondary variable pressure adsorption on the tail gas after primary variable pressure adsorption by using a secondary adsorbent.
The method comprises the following specific steps:
s1, compressing and condensing tail gas, compressing the tail gas under normal pressure to 0.8-1.2 MPa, condensing the compressed tail gas to 0 ℃, separating out first condensate, and then carrying out oil-water separation on the first condensate to obtain first condensate oil.
S2, when decarbonizing treatment is carried out on the compressed and condensed tail gas, absorbing carbon dioxide in the compressed and condensed tail gas by using a special absorbent for carbon dioxide; the carbon dioxide in the absorbent special for saturated carbon dioxide is removed and recovered, and the purity of the recovered carbon dioxide can reach 99 percent.
S3, performing primary pressure swing adsorption on the tail gas after the decarburization treatment, and further adsorbing light hydrocarbons in the tail gas after the decarburization treatment by using a primary adsorbent; condensing and regenerating the primary adsorbent to obtain a second condensate; and (3) carrying out oil-water separation on the second condensate liquid to obtain second condensate oil. Wherein, the primary adsorbent is a combined adsorption filler for separating high-efficiency high-boiling point substances.
S4, performing secondary pressure swing adsorption on the tail gas after primary pressure swing adsorption, and utilizing a secondary adsorbent to adsorb and separate methane and nitrogen in the tail gas after primary pressure swing adsorption, wherein the concentration of the separated nitrogen can reach 99%. Wherein the secondary adsorbent is a special efficient adsorbent for methane.
S5, performing secondary pressure swing adsorption on the tail gas subjected to primary pressure swing adsorption, and recycling residual pressure of the nitrogen obtained after the secondary pressure swing adsorption; and (3) carrying out pressure-variable adsorption on the second stage to obtain methane, and further concentrating to 90% by pressurization.
On the other hand, fig. 2 is a schematic diagram of a gas injection oil reservoir low hydrocarbon tail gas full separation recovery system according to the present invention, and as shown in fig. 2, the present invention also discloses a gas injection oil reservoir low hydrocarbon tail gas full separation recovery system, including a compression condensing device, a decarburization processing device, a primary pressure swing adsorption device and a secondary pressure swing adsorption device;
the compression condensing device is used for compressing and condensing the tail gas, and a gas outlet of the compression condensing device is connected with a gas inlet of the decarburization treatment device;
the decarbonization device is used for decarbonizing the compressed and condensed tail gas by matching with a special absorbent for carbon dioxide, and a gas outlet of the decarbonizing device is connected with a gas inlet of the primary pressure swing adsorption device;
the primary pressure swing adsorption device is used for carrying out primary pressure swing adsorption on the tail gas of the tail gas after decarburization treatment by matching with the primary adsorbent, and a gas outlet of the primary pressure swing adsorption device is connected with a gas inlet of the secondary pressure swing adsorption device;
The secondary pressure-variable adsorption device is used for carrying out secondary pressure-variable adsorption on the tail gas after primary pressure-variable adsorption by matching with the secondary adsorbent, and separating methane and nitrogen in the tail gas after primary pressure-variable adsorption, wherein the concentration of the separated nitrogen can reach 99%.
Further, a liquid outlet of the compression condensing device is connected with an inlet of a condensate recovery device, and the condensate recovery device is used for collecting first condensate generated by compression condensing tail gas;
The outlet of the condensate recovery device is connected with the inlet of the oil-water separation device, and the oil-water separation device is used for separating condensate oil and water in the condensate;
The condensate outlet of the oil-water separation device is connected with the inlet of a condensate storage tank, and the condensate storage tank is used for storing condensate.
Further, an absorbent outlet of the decarburization treatment device is connected with an inlet of an absorbent regeneration device, and the absorbent regeneration device is used for regenerating the absorbent special for saturated carbon dioxide and removing carbon dioxide in the absorbent special for saturated carbon dioxide;
The gas outlet of the absorbent regeneration device is connected with the inlet of the carbon dioxide recovery device, and the carbon dioxide recovery device is used for recovering the carbon dioxide removed by the absorbent special for regenerating the saturated carbon dioxide.
Further, an adsorbent outlet of the primary pressure swing adsorption device is connected with an inlet of the primary vacuum analysis device, a liquid outlet of the primary vacuum analysis device is connected with an inlet of the oil-water separation device, and the primary vacuum analysis device is used for analyzing and regenerating the saturated primary adsorbent to obtain second condensate;
The adsorbent outlet of the secondary variable pressure adsorption device is connected with the inlet of the secondary vacuum analysis device, and the secondary vacuum analysis device is used for analyzing and regenerating the saturated secondary adsorbent and removing methane.
Further, a gas outlet of the secondary variable pressure adsorption device is connected with a gas inlet of the methane concentration device, and the methane concentration device is used for pressurizing and concentrating methane to 90 percent concentration;
The outlet of the methane concentration device is connected with the inlet of the methane recovery device, and the methane recovery device is used for recovering, storing and pressurizing and concentrating methane.
Further, the solid outlets of the primary vacuum analysis device and the secondary vacuum analysis device are connected with the inlet of the enhanced regeneration device, the enhanced regeneration device is used for matching inert gas, the primary adsorbent and the secondary adsorbent are further regenerated in a mode of combining multiple regeneration modes, the regeneration efficiency and the service life of the adsorption material are guaranteed by adopting a high-strength regeneration mode under the protection of nitrogen, the adsorption equipment is guaranteed to be in an inert gas protection state during regeneration, fire hazards are avoided, and the regenerated bed layer is guaranteed to be in a low-temperature and dry favorable environment.
Further, the liquid outlet of the enhanced regeneration device is connected with the inlet of the oil-water separation device.
Through the low-hydrocarbon tail gas recovery system, low-concentration high-value light hydrocarbons and methane in the tail gas can be recovered, other gases such as nitrogen and carbon dioxide can be separated, the purity of the gases is high, the purity of the methane is higher than 90%, the purity of the nitrogen is higher than 99%, and the purity of the carbon dioxide is higher than 99%. On the one hand, the recovered gas can be sold, and if the tail gas amount is 200000Nm 3/d per day, about 30t of light hydrocarbon, methane 18000Nm 3/d, nitrogen 158400Nm 3/d and carbon dioxide 15840Nm 3/d can be recovered. The large-scale recovery system is built, the investment is 5500 ten thousand yuan, and each separated gas is sold according to market price, so that the cost can be recovered within two years. On the other hand, the recovered gas can be reinjected into oil fields, and is used for various tertiary oil recovery technologies, such as nitrogen foam flooding, carbon dioxide mixed phase flooding and the like. Meanwhile, the aim of carbon emission reduction can be achieved.
Finally, it should be noted that: the foregoing description is only illustrative of the preferred embodiments of the present invention, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements or changes may be made without departing from the spirit and principles of the present invention.
Claims (15)
1. The method for fully separating and recovering the low-hydrocarbon tail gas of the gas injection oil reservoir is characterized by comprising the following steps of:
Compressing and condensing the tail gas;
Decarburizing the tail gas after compression and condensation by using a special absorbent for carbon dioxide;
Performing primary pressure swing adsorption on the tail gas after decarburization treatment by using a primary adsorbent;
and carrying out secondary pressure swing adsorption on the tail gas subjected to the primary pressure swing adsorption by using a secondary adsorbent to obtain nitrogen.
2. The method for fully separating and recovering low hydrocarbon tail gas of a gas injection oil reservoir according to claim 1, wherein the step of condensing the tail gas by compression comprises the steps of:
Compressing the tail gas under normal pressure to 0.8-1.2 MPa;
and cooling the compressed tail gas to 0 ℃ to obtain a first condensate.
3. The method for fully separating and recovering low hydrocarbon tail gas from a gas injection oil reservoir according to claim 2, wherein after the tail gas is compressed and condensed, the method comprises the steps of:
and (3) oil-water separation is carried out on the first condensate liquid to obtain first condensate oil.
4. The method for fully separating and recovering low-hydrocarbon tail gas of a gas injection oil reservoir according to claim 1, wherein after the decarbonizing treatment of the tail gas after compression and condensation by using the carbon dioxide special absorbent, the method comprises the following steps:
And removing and recovering the carbon dioxide in the absorbent special for saturated carbon dioxide.
5. The method for fully separating and recovering low hydrocarbon tail gas from a gas injection oil reservoir according to claim 1, wherein after the decarburization treatment of the tail gas by using the primary adsorbent, the method comprises the steps of:
Condensing and regenerating the saturated primary adsorbent to obtain a second condensate;
and (3) carrying out oil-water separation on the second condensate liquid to obtain second condensate oil.
6. The method for fully separating and recycling low hydrocarbon tail gas of gas injection oil reservoir according to claim 5, wherein,
The primary adsorbent is a combined adsorption filler for separating high-boiling point substances.
7. The method for fully separating and recovering low hydrocarbon tail gas from a gas injection oil reservoir according to claim 1, wherein after the step of carrying out the second-stage pressure swing adsorption on the tail gas after the first-stage pressure swing adsorption by using the second-stage adsorbent, the method comprises the steps of:
The residual pressure recycling is carried out on the nitrogen obtained after the secondary variable pressure adsorption;
Regenerating the saturated secondary adsorbent to obtain methane;
Methane was concentrated to 90% under pressure.
8. The method for fully separating and recycling the low-hydrocarbon tail gas of the gas injection oil reservoir according to claim 7, which is characterized in that,
The secondary adsorbent is a special adsorbent for methane.
9. The system is characterized by comprising a compression condensing device, a decarburization treatment device, a primary pressure swing adsorption device and a secondary pressure swing adsorption device;
The compression condensing device is used for compressing and condensing tail gas, and a gas outlet of the compression condensing device is connected with a gas inlet of the decarburization treatment device;
The decarbonization device is used for decarbonizing the tail gas after compression and condensation by matching with a special absorbent for carbon dioxide, and a gas outlet of the decarbonizing device is connected with a gas inlet of the primary pressure swing adsorption device;
The primary pressure swing adsorption device is used for carrying out primary pressure swing adsorption on the tail gas after decarburization treatment by matching with the primary adsorbent, and a gas outlet of the primary pressure swing adsorption device is connected with a gas inlet of the secondary pressure swing adsorption device;
The secondary pressure-variable adsorption device is used for carrying out secondary pressure-variable adsorption on the tail gas after primary pressure-variable adsorption by matching with a secondary adsorbent to obtain nitrogen.
10. The gas injection oil reservoir low hydrocarbon tail gas full separation recovery system according to claim 9, wherein,
The liquid outlet of the compression condensing device is connected with the inlet of the condensate recovery device, and the condensate recovery device is used for collecting first condensate generated by compression condensing tail gas;
The outlet of the condensate recovery device is connected with the inlet of the oil-water separation device, and the oil-water separation device is used for separating condensate oil and water in the condensate;
the condensate outlet of the oil-water separation device is connected with the inlet of a condensate storage tank, and the condensate storage tank is used for storing condensate.
11. The gas injection oil reservoir low hydrocarbon tail gas full separation recovery system according to claim 9, wherein,
The absorbent outlet of the decarburization treatment device is connected with the inlet of an absorbent regeneration device, and the absorbent regeneration device is used for regenerating the absorbent special for saturated carbon dioxide and removing carbon dioxide in the absorbent special for saturated carbon dioxide;
the gas outlet of the absorbent regeneration device is connected with the inlet of the carbon dioxide recovery device, and the carbon dioxide recovery device is used for recovering the carbon dioxide removed by the absorbent special for saturated carbon dioxide.
12. The gas injection oil pool low hydrocarbon tail gas full separation recovery system according to claim 10, wherein,
The adsorbent outlet of the primary pressure swing adsorption device is connected with the inlet of the primary vacuum analysis device, the liquid outlet of the primary vacuum analysis device is connected with the inlet of the oil-water separation device, and the primary vacuum analysis device is used for analyzing and regenerating the saturated primary adsorbent to obtain second condensate;
And an adsorbent outlet of the secondary variable pressure adsorption device is connected with an inlet of a secondary vacuum analysis device, and the secondary vacuum analysis device is used for analyzing and regenerating the saturated secondary adsorbent and removing methane.
13. The gas injection oil pool low hydrocarbon tail gas full separation recovery system according to claim 12, wherein,
The gas outlet of the secondary variable pressure adsorption device is connected with the gas inlet of the methane concentration device, and the methane concentration device is used for pressurizing and concentrating methane to 90 percent concentration;
The outlet of the methane concentration device is connected with the inlet of the methane recovery device, and the methane recovery device is used for recovering, storing and pressurizing and concentrating methane.
14. The gas injection oil pool low hydrocarbon tail gas full separation recovery system according to claim 13, wherein,
The adsorbent outlets of the primary vacuum analysis device and the secondary vacuum analysis device are connected with the inlet of the enhanced regeneration device, and the enhanced regeneration device is used for carrying out further regeneration treatment on the primary adsorbent and the secondary adsorbent in a mode of combining a plurality of regeneration modes by matching with inert gas.
15. The gas injection oil pool low hydrocarbon tail gas full separation recovery system according to claim 14, wherein,
The liquid outlet of the enhanced regeneration device is connected with the inlet of the oil-water separation device.
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| CN202211428595.1A CN118045388A (en) | 2022-11-15 | 2022-11-15 | Gas injection oil reservoir low-hydrocarbon tail gas full-separation recovery method and system |
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