CN114702992A - Separation and purification system and method for carbon dioxide-containing produced gas in oil field - Google Patents
Separation and purification system and method for carbon dioxide-containing produced gas in oil field Download PDFInfo
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- CN114702992A CN114702992A CN202111681422.6A CN202111681422A CN114702992A CN 114702992 A CN114702992 A CN 114702992A CN 202111681422 A CN202111681422 A CN 202111681422A CN 114702992 A CN114702992 A CN 114702992A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 448
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 224
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 224
- 238000000746 purification Methods 0.000 title claims abstract description 192
- 238000000926 separation method Methods 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 146
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract description 85
- 230000020335 dealkylation Effects 0.000 claims abstract description 48
- 238000006900 dealkylation reaction Methods 0.000 claims abstract description 48
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 40
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 40
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000003345 natural gas Substances 0.000 claims abstract description 11
- 239000006096 absorbing agent Substances 0.000 claims abstract description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 abstract description 7
- 230000006835 compression Effects 0.000 abstract description 4
- 238000007906 compression Methods 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 239000001294 propane Substances 0.000 description 8
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- 239000012528 membrane Substances 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 101100134058 Caenorhabditis elegans nth-1 gene Proteins 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003498 natural gas condensate Substances 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
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- Oil, Petroleum & Natural Gas (AREA)
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- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
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Abstract
The invention discloses a separation and purification system and a method for carbon dioxide-containing produced gas in an oil field, which belong to the field of recovery of the produced gas in the oil field, and comprise a compressor, a desulfurizer, a dryer, a precooler, a dealkylation tower, a multi-stage alkane separation and purification tower, a condenser, a multi-stage carbon dioxide purification tower, a subcooler and a pressure swing absorber; the invention compresses, desulfurizes and dries the produced gas rich in carbon dioxide separated from oil field oil extraction, and sends it into precooler to cool, and then sends it into de-hydrocarbon tower, and the removed hydrocarbon sends it into multi-stage alkane separating and purifying tower, to obtain high-purity light component and heavy component. The gas from the de-hydrocarbon tower is rectified in multiple stages to obtain carbon dioxide liquid which can be injected back into oil field to displace oil, the gas removed by the multiple stages of rectification is subjected to pressure swing adsorption to remove carbon dioxide to obtain high-purity natural gas, the carbon dioxide-rich gas removed by the pressure swing adsorption flows back to be mixed with the produced gas before compression to be used as raw material gas, and no tail gas or mixed gas is discharged.
Description
Technical Field
The invention relates to the field of recovery of produced gas in an oil field, in particular to a system and a method for separating and purifying produced gas containing carbon dioxide in the oil field.
Background
With the development of oil field exploitation technology, carbon dioxide flooding is more and more widely applied, when a large amount of carbon dioxide is injected into an oil well for flooding, the content of carbon dioxide in components of gas produced by a certain well mouth is gradually increased, and the produced gas rich in carbon dioxide is difficult to be effectively utilized.
At present, widely applied separation and purification processes of gas produced at a wellhead comprise a membrane separation method and a low-temperature methanol washing method. The invention of China patent CN104857811A discloses a system for separating and recovering carbon dioxide from oil field carbon dioxide flooding produced gas, which adopts a membrane separation method, can realize coarse and fine separation of carbon dioxide from produced gas with higher carbon dioxide concentration based on the arrangement of an oil-gas separation tower, a first compressor, a cooler, a condensation filter, a heat exchanger, an activated carbon adsorption bed, a particle filter, a heater, a second compressor and a membrane separation device, is suitable for separating the carbon dioxide from the produced gas of a single well, is suitable for separating and recovering the carbon dioxide from the produced gas of small and medium scales in the oil field, but the membrane separation technology needs multistage compression and a membrane separator for separating the produced gas containing the carbon dioxide, and has high construction cost. The separated natural gas component contains about 20% of carbon dioxide and cannot be commercialized. The high added value propane, butane and heavy hydrocarbon contained in the produced gas can not be effectively separated and purified, and the economic benefit is poor. The process has no desulfurization, and the product rich carbon dioxide liquid phase contains more hydrogen sulfide and has higher harm to a rear-end injection well oil displacement system. US patent 11674083 discloses a natural gas processing system employing a cryogenic methanol wash separation technique to dehydrate and cool a carbon dioxide containing produced natural gas to liquefy the carbon dioxide, which is then fractionated to produce a waste stream of liquid carbon dioxide and hydrogen sulfide. The natural gas condensate may first be separated and removed prior to fractionation. After fractionation, the waste stream is pressurized and transferred to an injection well at a distance for injection or disposal of the waste stream, and preferably for pushing hydrocarbons towards a production well. A hydrocarbon stream is passed from the fractionation column to a methanol absorber system that removes carbon dioxide gas. The hydrocarbon stream is then separated into at least hydrocarbon gas, nitrogen and helium. Some nitrogen is reintroduced into the fractionator to increase hydrocarbon recovery, but this technique requires a large amount of refrigeration at-45 ℃ and is costly to consume. Propane, butane and heavy hydrocarbon with high added value in the produced gas can not be separated, and the economic benefit is poor. The process has no desulfurization, and the product rich carbon dioxide liquid phase contains more hydrogen sulfide and has higher harm to a rear-end injection well oil displacement system.
Disclosure of Invention
In view of the above defects in the prior art, the technical problem to be solved by the invention is how to realize high-efficiency low-energy-consumption recovery of all produced gas, thereby purifying and separating natural gas with commercial grade purity, light components and heavy components, and being suitable for liquid carbon dioxide for oil displacement of oil fields.
In order to achieve the purpose, the invention provides an oil field carbon dioxide-containing produced gas separation and purification system which is characterized by comprising a compressor, a desulfurizer, a dryer, a precooler, a dealkylation tower, a multi-stage alkane separation and purification tower, a condenser, a multi-stage carbon dioxide purification tower, a subcooler and a pressure swing adsorber; the precooler comprises a raw material gas inlet, a raw material gas outlet, a carbon dioxide purification tail gas inlet and a carbon dioxide purification tail gas outlet; the inlet of the desulfurizer is connected with the outlet of the compressor, the inlet of the dryer is connected with the outlet of the desulfurizer, the inlet of the precooler raw material gas is connected with the dryer, the inlet of the dealkylation tower is connected with the outlet of the precooler raw material gas, the inlet of the multistage alkane separation and purification tower is connected with the lower outlet of the dealkylation tower, the inlet of the multistage carbon dioxide purification tower is connected with the upper outlet of the dealkylation tower, the upper outlet of the multistage carbon dioxide purification tower is connected with the inlet of the carbon dioxide purification tail gas of the precooler, the outlet of the carbon dioxide purification tail gas of the precooler is connected with the inlet of the pressure swing adsorber, and the outlet of the carbon dioxide-rich tail gas of the pressure swing adsorber is connected with the inlet of the compressor;
and an outlet at the upper part of the multistage alkane separation and purification tower is connected with the condenser, and an outlet at the lower part of the multistage carbon dioxide purification tower is connected with the subcooler.
Further, a condenser of the hydrocarbon removing tower is arranged at the top of the hydrocarbon removing tower, and a reboiler of the hydrocarbon removing tower is arranged at the bottom of the hydrocarbon removing tower; and an outlet at the upper part of the dealkylation tower is connected with an inlet of the multistage carbon dioxide purification tower through the dealkylation tower condenser, and an outlet at the lower part of the dealkylation tower is connected with an inlet of the multistage alkane separation and purification tower through the dealkylation tower reboiler.
Furthermore, the multi-stage alkane separation and purification tower has m (m is more than or equal to 1) stages, the top of each stage of alkane separation and purification tower is provided with an alkane separation and purification tower condenser, and the bottom of each stage of alkane separation and purification tower is provided with an alkane separation and purification tower reboiler; wherein, the upper outlet of the m-grade alkane separating and purifying tower in the multi-grade alkane separating and purifying tower is connected with the inlet of the condenser through the condenser of the m-grade alkane separating and purifying tower; the upper outlets of other alkane separating and purifying towers at each stage are connected with the lower alkane separating and purifying tower through the alkane separating and purifying tower condenser.
Furthermore, the multi-stage carbon dioxide purification tower has n (n is more than or equal to 2) stages, the top of each stage is provided with a carbon dioxide purification tower condenser, and the bottom is provided with a carbon dioxide purification tower reboiler; the upper outlet of the front-stage carbon dioxide purification tower is connected with the inlet of the rear-stage carbon dioxide purification tower through a condenser of the front-stage carbon dioxide purification tower, the upper outlet of the n-stage carbon dioxide purification tower is connected with the inlet of the carbon dioxide purification tail gas of the precooler through the condenser of the n-stage carbon dioxide purification tower, and the lower outlet of the multi-stage carbon dioxide purification tower is connected with the inlet of the subcooler through a reboiler of the multi-stage carbon dioxide purification tower.
The invention provides another aspect of a separation and purification method for produced gas containing carbon dioxide in an oil field, which comprises the following steps:
s10, pressurizing produced gas from an oil field by a compressor;
s20, removing sulfur from the pressurized produced gas through a desulfurizer;
s30, removing moisture from the produced gas from the desulfurizer through a dryer;
s40, cooling the produced gas from the dryer through a precooler;
s50, introducing produced gas from the precooler into the middle part of a dealkylation tower, providing a cold source by a condenser of the dealkylation tower, providing a heat source by a reboiler of the dealkylation tower, and providing alkanes with more than C2 at an outlet of the reboiler of the dealkylation tower; the outlet of the condenser of the dealkylation tower is a mixed gas of carbon dioxide and methane;
s60, feeding a mixed gas of carbon dioxide and methane from an outlet of a condenser of a dealkylation tower into a first-stage carbon dioxide purification tower in a multi-stage carbon dioxide purification tower, wherein the condenser of the first-stage carbon dioxide purification tower at the top provides a cold source, the outlet of the condenser of the first-stage carbon dioxide purification tower provides first non-condensable gas, a reboiler of the first-stage carbon dioxide purification tower at the bottom provides a heat source, and the outlet of the reboiler of the first-stage carbon dioxide purification tower provides liquid carbon dioxide;
s70, feeding the first non-condensable gas from the outlet of the condenser of the first-stage carbon dioxide purification tower into a second-stage carbon dioxide purification tower, wherein the condenser of the second-stage carbon dioxide purification tower at the top provides a cold source, the outlet of the condenser of the second-stage carbon dioxide purification tower provides the second non-condensable gas, a reboiler of the second-stage carbon dioxide purification tower at the bottom provides a heat source, and the outlet of the reboiler of the second-stage carbon dioxide purification tower at the bottom is liquid carbon dioxide;
s80, feeding the nth-1 non-condensable gas from the outlet of the condenser of the nth-1 level carbon dioxide purification tower into the nth level carbon dioxide purification tower, wherein the condenser of the nth level carbon dioxide purification tower at the top provides a cold source, the outlet of the condenser of the nth level carbon dioxide purification tower provides the nth non-condensable gas, the reboiler of the nth level carbon dioxide purification tower at the bottom provides a heat source, and the outlet of the reboiler of the nth level carbon dioxide purification tower at the bottom is liquid carbon dioxide;
s90, mixing carbon dioxide from the first-stage carbon dioxide purification tower and carbon dioxide from the second-stage carbon dioxide purification tower until carbon dioxide from the n-stage carbon dioxide purification tower enters a subcooler, and discharging a subcooled liquid carbon dioxide product from the subcooler;
s100, the nth non-condensable gas enters a precooler to recycle cold, and the outlet of the precooler is the (n + 1) th non-condensable gas;
s110, feeding the n +1 th non-condensable gas into a pressure swing adsorber, wherein a tail gas outlet of the pressure swing adsorber is a carbon dioxide-rich tail gas, the carbon dioxide-rich tail gas is mixed with produced gas from an oil field through gas-liquid-solid separation and is used as raw material gas to enter a compressor, and a product outlet of the pressure swing adsorber is used as product natural gas.
Further, the method also comprises the following steps:
s120, enabling mixed liquid from an outlet of a reboiler of the dealkylation tower to enter a first-stage alkane separation and purification tower in a multi-stage alkane separation and purification tower, enabling a condenser of the first-stage alkane separation and purification tower to provide a cold source, enabling a reboiler of the first-stage alkane separation and purification tower to provide a heat source, enabling an outlet of each stage of condenser of the multi-stage alkane separation and purification tower to be light hydrocarbons with different components, enabling the light hydrocarbons to enter a next-stage alkane separation and purification tower for further separation, enabling an outlet of an m-stage alkane separation and purification tower to be high-purity light hydrocarbons, and enabling an outlet of the reboiler of each stage of alkane separation and purification tower to be heavy hydrocarbons with different types;
s130, condensing high-purity light hydrocarbon from the outlet of the condenser of the n-level alkane separation and purification tower through the condenser, wherein the outlet of the condenser is the product liquid high-purity light hydrocarbon.
The invention has the beneficial effects that:
the invention compresses, desulfurizes and dries the produced gas rich in carbon dioxide separated from oil field oil extraction, and sends it into precooler to cool, and then sends it into de-hydrocarbon tower, and the removed hydrocarbon sends it into multi-stage alkane separating and purifying tower, to obtain high-purity light component and heavy component. The gas from the de-hydrocarbon tower is rectified to obtain carbon dioxide liquid which can be injected back into the oil field to displace oil, the gas removed by the multi-stage rectification is subjected to pressure swing adsorption to remove carbon dioxide to obtain high-purity natural gas, the carbon dioxide-rich gas removed by the pressure swing adsorption is refluxed to the compression stage and mixed with the produced gas to be used as raw material gas, and no tail gas or mixed gas is discharged.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a system flow diagram of a preferred embodiment of the present invention.
In the figure: 1. a compressor; 2. a desulfurizer; 3. a dryer; 4. a precooler; 5. a de-hydrocarbon tower; 51. a de-hydrocarbon tower condenser; 52. a de-hydrocarbonation column reboiler; 6. a first-stage carbon dioxide purification tower; 61. a first-stage carbon dioxide purification tower condenser; 62. a reboiler of the first-stage carbon dioxide purification tower; 7. a secondary carbon dioxide purification tower; 71. a secondary carbon dioxide purification tower condenser; 72. a secondary carbon dioxide purification tower reboiler; 8. an n-1 stage carbon dioxide purification tower; 81. an n-1 stage carbon dioxide purification tower condenser; 82. an n-1 stage carbon dioxide purification tower reboiler; 9. n-stage carbon dioxide purification tower; 91. n-stage carbon dioxide purification tower condenser; 92. an n-stage carbon dioxide purification tower reboiler; 10. a pressure swing adsorber; 11. a first-stage alkane separation and purification tower; 111. a first-stage alkane separating and purifying tower condenser; 112. a reboiler of the first-stage alkane separation and purification tower; 12. a second-stage alkane separation and purification tower; 121. a condenser of a second-level alkane separation and purification tower; 122. a reboiler of the second-level alkane separation and purification tower; 13. an m-grade alkane separating and purifying tower; 131. m-grade alkane separation and purification tower condenser; 132. a reboiler of the m-grade alkane separation and purification tower; 14. a subcooler; 15. a condenser.
Detailed Description
The technical contents of the preferred embodiments of the present invention will be more clearly and easily understood by referring to the drawings attached to the specification. The present invention may be embodied in many different forms of embodiments and the scope of the invention is not limited to the embodiments set forth herein.
Example 1
In the drawings, structurally identical elements are represented by like reference numerals, and structurally or functionally similar elements are represented by like reference numerals throughout the several views. The size and thickness of each component shown in the drawings are arbitrarily illustrated, and the present invention is not limited to the size and thickness of each component. The thickness of the components may be exaggerated where appropriate in the figures to improve clarity.
In a preferred embodiment of the present invention, as shown in fig. 1, the system for separating and purifying carbon dioxide-containing produced gas in an oil field comprises a compressor 1, a desulfurizer 2, a dryer 3, a precooler 4, a dealkylation tower 5, a multi-stage alkane separating and purifying tower, a condenser 15, a multi-stage carbon dioxide purifying tower, a subcooler 14 and a pressure swing adsorber 11.
The precooler 4 is a heat exchanger or an evaporative cooler for reducing the temperature of the working medium before the working medium starts to be compressed, and comprises a raw material gas inlet, a raw material gas outlet, a carbon dioxide purification tail gas inlet and a carbon dioxide purification tail gas outlet.
The condenser 15 is a type of heat exchanger that converts gas or vapor into liquid and transfers the heat of the heat source to the heat sink in a quick manner. The condenser operation is an exothermic process.
The subcooler 14 is a heat exchanger that further cools the saturated liquid without phase change.
As shown in fig. 1, an inlet of a desulfurizer 2 is connected with an outlet of a compressor 1, an inlet of a dryer 3 is connected with an outlet of the desulfurizer 2, a raw material gas inlet of a precooler 4 is connected with the dryer 3, an inlet of a dealkylation tower 5 is connected with a raw material gas outlet of the precooler 4, an inlet of a multistage alkane separation and purification tower is connected with a lower outlet of the dealkylation tower 5, an inlet of a multistage carbon dioxide purification tower is connected with an upper outlet of the dealkylation tower 5, an upper outlet of the multistage carbon dioxide purification tower is connected with a carbon dioxide purification tail gas inlet of the precooler 4, a carbon dioxide purification tail gas outlet of the precooler 4 is connected with an inlet of a pressure swing adsorber 10, and a carbon dioxide-rich tail gas outlet of the pressure swing adsorber 10 is connected with an inlet of the compressor 1; the upper outlet of the multi-stage alkane separating and purifying tower is connected with the condenser 15, and the lower outlet of the multi-stage carbon dioxide purifying tower is connected with the subcooler 14.
As shown in fig. 1, in the preferred embodiment of the present invention, the dealkylation column 5 has a dealkylation column condenser 51 at the top and a dealkylation column reboiler 52 at the bottom; an outlet at the upper part of the dealkylation tower 5 is connected with an inlet of the multi-stage carbon dioxide purification tower through a condenser 51 of the dealkylation tower, and an outlet at the lower part of the dealkylation tower 5 is connected with an inlet of the multi-stage alkane separation and purification tower through a reboiler 52 of the dealkylation tower.
As shown in fig. 1, in the preferred embodiment of the present invention, the multi-stage alkane separating and purifying tower has 3 stages, the top of each stage of alkane separating and purifying tower is provided with an alkane separating and purifying tower condenser, and the bottom is provided with an alkane separating and purifying tower reboiler; wherein the upper outlet of the third alkane separating and purifying tower in the multistage alkane separating and purifying tower is connected with the inlet of the condenser 15 through the condenser of the third alkane separating and purifying tower; the upper outlets of other alkane separating and purifying towers at each stage are connected with the lower alkane separating and purifying tower through the alkane separating and purifying tower condenser.
As shown in fig. 1, in the preferred embodiment of the present invention, the multi-stage carbon dioxide purification tower has 4 stages, each stage having a condenser at the top of the carbon dioxide purification tower and a reboiler at the bottom of the carbon dioxide purification tower; wherein, the upper outlet of the front-stage carbon dioxide purification tower is connected with the inlet of the rear-stage carbon dioxide purification tower through the condenser of the front-stage carbon dioxide purification tower; an outlet at the upper part of the four-stage carbon dioxide purification tower is connected with an inlet of the carbon dioxide purification tail gas of the precooler 4 through a condenser of the four-stage carbon dioxide purification tower, and outlets at the lower part of all the carbon dioxide purification towers are connected with an inlet of the subcooler 14 through a reboiler of the carbon dioxide purification tower.
Example 2
For better purification, in another preferred embodiment of the present invention, the multi-stage paraffin separation and purification tower has 4 stages and the multi-stage carbon dioxide purification tower has 6 stages.
Example 3
In order to match the implementation of the embodiment, the invention provides a matched separation and purification method for produced gas containing carbon dioxide in an oil field, which specifically comprises the following steps:
s10, pressurizing produced gas from an oil field by a compressor 1; wherein, the oil field is subjected to gas-liquid-solid separation to obtain the molar components of the produced gas: 68% carbon dioxide, 2% methane, 3% ethane, 3% propane, 2% n-butane, 0.5% hydrogen sulfide, 0.5% nitrogen, 3% water.
S20, removing sulfur from the pressurized produced gas through a desulfurizer 2;
s30, removing moisture from the produced gas from the desulfurizer 2 through a dryer 3;
s40, cooling the produced gas from the dryer 3 through the precooler 4;
s50, enabling produced gas from the precooler 4 to enter the middle part of a dealkylation tower 5, enabling a condenser 51 of the dealkylation tower to provide a cold source, enabling a reboiler 52 of the dealkylation tower to provide a heat source, and enabling an outlet of the reboiler 52 of the dealkylation tower to be hydrocarbon with the carbon number of more than 2; the outlet of the condenser 51 of the dealkylation tower is a mixed gas of carbon dioxide, methane and the like; wherein, C2 is the mole component of the following hydrocarbons: 1.29% carbon dioxide, 0.01% ethane, 53.72% propane, 44.97% n-butane.
S60, feeding the mixed gas of carbon dioxide and methane from the outlet of the condenser 51 of the dealkylation tower into a first-stage carbon dioxide purification tower 6 of a multi-stage carbon dioxide purification tower, wherein the condenser 61 of the first-stage carbon dioxide purification tower at the top provides a cold source, the outlet of the condenser 61 of the first-stage carbon dioxide purification tower provides a first non-condensable gas, the reboiler 62 of the first-stage carbon dioxide purification tower at the bottom provides a heat source, and the outlet of the reboiler 62 of the first-stage carbon dioxide purification tower provides liquid carbon dioxide;
s70, feeding the first non-condensable gas from the outlet of the condenser 61 of the first-stage carbon dioxide purification tower into a second-stage carbon dioxide purification tower 7, wherein a cold source is provided by a condenser 71 of the second-stage carbon dioxide purification tower at the top, the second non-condensable gas is provided by the outlet of the condenser 71 of the second-stage carbon dioxide purification tower, a heat source is provided by a reboiler 72 of the second-stage carbon dioxide purification tower at the bottom, and liquid carbon dioxide is provided by the outlet of the reboiler 72 of the second-stage carbon dioxide purification tower at the bottom;
s80, feeding the n-1 th non-condensable gas from the outlet of the condenser 81 of the n-1 stage carbon dioxide purification tower into an n-stage carbon dioxide purification tower 9, wherein a cold source is provided by the condenser 91 of the n-stage carbon dioxide purification tower at the top, the n-th non-condensable gas is provided by the outlet of the condenser 92 of the n-stage carbon dioxide purification tower, a heat source is provided by the reboiler 92 of the n-stage carbon dioxide purification tower at the bottom, and liquid carbon dioxide is provided by the outlet of the reboiler 92 of the n-stage carbon dioxide purification tower at the bottom;
s90, mixing the carbon dioxide from the first-stage carbon dioxide purification tower 6, the carbon dioxide from the second-stage carbon dioxide purification tower 7 and the carbon dioxide from the n-stage carbon dioxide purification tower 9, and allowing the mixture to enter a subcooler 14, wherein the outlet of the subcooler 14 is a product subcooled liquid carbon dioxide; wherein, the molar composition of the super-cooled carbon dioxide is as follows: 95.71% carbon dioxide, 1.34% methane, 2.09% ethane, 0.86% propane.
S100, the nth non-condensable gas enters a precooler 4 to recover cold, and the outlet of the nth non-condensable gas is the (n + 1) th non-condensable gas;
s110, enabling the n +1 th non-condensable gas to enter a pressure swing adsorber 10, enabling a tail gas outlet of the pressure swing adsorber 10 to be a carbon dioxide-rich tail gas, enabling the carbon dioxide-rich tail gas and produced gas from an oil field after gas-liquid-solid separation to be mixed to serve as raw material gas to enter a compressor 1, and enabling a product outlet of the pressure swing adsorber 10 to be product natural gas; wherein, the molar composition of the product natural gas is as follows: 90.4% methane, 7.22% ethane, 2.37% nitrogen; molar composition of the carbon dioxide rich tail gas: 84.48% carbon dioxide, 8.32% methane, 5.41% ethane, 0.01 propane, 1.78% nitrogen.
S120, enabling mixed liquid from an outlet of a reboiler 52 of the dealkylation tower to enter a first-stage alkane separation and purification tower 11 in a multi-stage alkane separation and purification tower, enabling a condenser 111 of the first-stage alkane separation and purification tower to provide a cold source, enabling a reboiler 112 of the first-stage alkane separation and purification tower to provide a heat source, enabling an outlet of each stage of condenser of the multi-stage alkane separation and purification tower to be light hydrocarbons with different components, enabling the light hydrocarbons to enter a next-stage alkane separation and purification tower for further separation, enabling an outlet of an m-stage alkane separation and purification tower to be high-purity light hydrocarbons, and enabling an outlet of a reboiler of each stage of alkane separation and purification tower to be heavy hydrocarbons; wherein, the molar components of the high-purity light hydrocarbon are as follows: 2.51% carbon dioxide, 0.033% ethane, 97.46% propane, 0.01% n-butane; molar composition of heavy hydrocarbons: 7.39% propane, 92.61% n-butane.
S130, condensing high-purity light hydrocarbon from an outlet of a condenser 131 of the n-grade alkane separation and purification tower through a condenser 15, wherein the outlet of the condenser 15 is the high-purity light hydrocarbon of the product liquid.
The invention compresses, desulfurizes and dries the produced gas rich in carbon dioxide separated from oil field oil extraction, and sends it into precooler to cool, and then sends it into de-hydrocarbon tower, and the removed hydrocarbon sends it into alkane separating and purifying tower, to obtain high-purity light component and heavy component. The gas from the de-hydrocarbon tower is purified through two-stage rectification to obtain carbon dioxide liquid which can be injected back into the oil field to displace oil, the gas removed through two-stage rectification is subjected to pressure swing adsorption to remove carbon dioxide to obtain high-purity natural gas, the carbon dioxide-rich gas removed through pressure swing adsorption is refluxed to the front of compression and mixed with the produced gas to be used as raw material gas, and no tail gas or mixed gas is discharged.
The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.
Claims (6)
1. The system for separating and purifying the produced gas containing carbon dioxide in the oil field is characterized by comprising a compressor (1), a desulfurizer (2), a dryer (3), a precooler (4), a dealkylation tower (5), a multi-stage alkane separating and purifying tower, a condenser (15), a multi-stage carbon dioxide purifying tower, a subcooler (14) and a pressure swing adsorber (11);
the precooler (4) comprises a raw material gas inlet, a raw material gas outlet, a carbon dioxide purification tail gas inlet and a carbon dioxide purification tail gas outlet;
wherein the inlet of the desulfurizer (2) is connected with the outlet of the compressor (1), the inlet of the dryer (3) is connected with the outlet of the desulfurizer (2), the feed gas inlet of the precooler (4) is connected with the dryer (3), the inlet of the dealkylation tower (5) is connected with the feed gas outlet of the precooler (4), the inlet of the multi-stage alkane separating and purifying tower is connected with the outlet at the lower part of the dealkylation tower (5), the inlet of the multi-stage carbon dioxide purification tower is connected with the outlet at the upper part of the dealkylation tower (5), the outlet at the upper part of the multi-stage carbon dioxide purification tower is connected with the inlet of the carbon dioxide purification tail gas of the precooler (4), the outlet of the carbon dioxide purification tail gas of the precooler (4) is connected with the inlet of the pressure swing absorber (10), the outlet of the pressure swing adsorber (10) rich in carbon dioxide tail gas is connected with the inlet of the compressor (1);
the upper outlet of the multistage alkane separation and purification tower is connected with the condenser (15), and the lower outlet of the multistage carbon dioxide purification tower is connected with the subcooler (14).
2. The system for separating and purifying the carbon dioxide-containing produced gas in the oil field according to the claim 1, wherein the top of the hydrocarbon removing tower (5) is provided with a hydrocarbon removing tower condenser (51), and the bottom is provided with a hydrocarbon removing tower reboiler (52);
the upper outlet of the dealkylation tower (5) is connected with the inlet of the multi-stage carbon dioxide purification tower through the dealkylation tower condenser (51), and the lower outlet of the dealkylation tower (5) is connected with the inlet of the multi-stage alkane separation and purification tower through the dealkylation tower reboiler (52).
3. The system for separating and purifying the carbon dioxide-containing produced gas in the oil field as claimed in claim 1, wherein the multi-stage alkane separation and purification tower has m (m is more than or equal to 1) stages, the top of each stage of alkane separation and purification tower is provided with an alkane separation and purification tower condenser (111, 121, 131), and the bottom is provided with an alkane separation and purification tower reboiler (112, 122, 132);
wherein, the upper outlet of the m-grade alkane separating and purifying tower (13) in the multi-grade alkane separating and purifying tower is connected with the inlet of the condenser (15) through a condenser (131) of the m-grade alkane separating and purifying tower; the upper outlets of other alkane separating and purifying towers at each stage are connected with the lower alkane separating and purifying tower through the alkane separating and purifying tower condenser.
4. The system for separating and purifying the carbon dioxide-containing produced gas in the oil field according to claim 1, wherein the multistage carbon dioxide purifying tower comprises n (n is more than or equal to 2) stages, a condenser (61, 71, 81, 91) of the carbon dioxide purifying tower is arranged at the top of each stage, and a reboiler (62, 72, 82, 92) of the carbon dioxide purifying tower is arranged at the bottom of each stage;
wherein, the outlet of the upper part of the preceding carbon dioxide purification tower is connected with the inlet of the subsequent carbon dioxide purification tower through the condenser of the preceding carbon dioxide purification tower, the outlet of the upper part of the n-stage carbon dioxide purification tower (9) is connected with the inlet of the carbon dioxide purification tail gas of the precooler (4) through the condenser (91) of the n-stage carbon dioxide purification tower, and the outlet of the lower part of the multi-stage carbon dioxide purification tower is connected with the inlet of the subcooler (14) through the reboiler of the multi-stage carbon dioxide purification tower.
5. A method for separating and purifying produced gas containing carbon dioxide in an oil field is characterized by comprising the following steps:
s10, pressurizing produced gas from an oil field by a compressor (1);
s20, removing sulfur from the pressurized produced gas through a desulfurizer (2);
s30, removing moisture from the produced gas from the desulfurizer (2) through a dryer (3);
s40, cooling the produced gas from the dryer (3) through a precooler (4);
s50, introducing produced gas from the precooler (4) into the middle part of a dealkylation tower (5), wherein a condenser (51) of the dealkylation tower provides a cold source, a reboiler (52) of the dealkylation tower provides a heat source, and the outlet of the reboiler (52) of the dealkylation tower is alkane with more than C2; the outlet of the condenser (51) of the hydrocarbon removing tower is a mixed gas of carbon dioxide and methane;
s60, feeding a mixed gas of carbon dioxide and methane from an outlet of a condenser (51) of a dealkylation tower into a first-stage carbon dioxide purification tower (6) in a multi-stage carbon dioxide purification tower, wherein a cold source is provided by a condenser (61) at the top of the first-stage carbon dioxide purification tower, a first non-condensable gas is provided by an outlet of a condenser (61) of a primary carbon dioxide purification tower, a heat source is provided by a reboiler (62) at the bottom of the first-stage carbon dioxide purification tower, and liquid carbon dioxide is provided by an outlet of the reboiler (62) of the first-stage carbon dioxide purification tower;
s70, feeding the first non-condensable gas from an outlet of a condenser (61) of the first-stage carbon dioxide purification tower into a second-stage carbon dioxide purification tower (7), wherein a cold source is provided by a condenser (71) of the top second-stage carbon dioxide purification tower, the second non-condensable gas is provided by an outlet of the condenser (71) of the second-stage carbon dioxide purification tower, a heat source is provided by a reboiler (72) of the bottom second-stage carbon dioxide purification tower, and liquid carbon dioxide is provided by an outlet of the reboiler (72) of the bottom second-stage carbon dioxide purification tower;
s80, feeding the n-1 th non-condensable gas from the outlet of the condenser (81) of the n-1 stage carbon dioxide purification tower into an n-stage carbon dioxide purification tower (9), wherein a cold source is provided by the condenser (91) of the n-stage carbon dioxide purification tower at the top, the outlet of the condenser (91) of the n-stage carbon dioxide purification tower is used for providing the n-th non-condensable gas, a heat source is provided by the reboiler (92) of the n-stage carbon dioxide purification tower at the bottom, and liquid carbon dioxide is provided by the outlet of the reboiler (92) of the n-stage carbon dioxide purification tower at the bottom;
s90, mixing carbon dioxide from the first-stage carbon dioxide purification tower (6), carbon dioxide from the second-stage carbon dioxide purification tower (7) and carbon dioxide from the n-stage carbon dioxide purification tower (9), and allowing the mixture to enter a subcooler (14), wherein the outlet of the subcooler (14) is a product subcooled liquid carbon dioxide;
s100, enabling the nth non-condensable gas to enter a precooler (4) for recovering cold, and enabling the nth +1 th non-condensable gas to be at an outlet;
s110, the n +1 th non-condensable gas enters a pressure swing absorber (10), a tail gas outlet of the pressure swing absorber (10) is carbon dioxide-rich tail gas, the carbon dioxide-rich tail gas and produced gas from an oil field after gas-liquid-solid separation are mixed to serve as raw material gas to enter a compressor (1), and a product outlet of the pressure swing absorber (10) is product natural gas.
6. The method of claim 5, further comprising the steps of:
s120, mixed liquid from an outlet of a reboiler (52) of the dealkylation tower enters a first-stage alkane separation and purification tower (11) in a multi-stage alkane separation and purification tower, a condenser (111) of the first-stage alkane separation and purification tower provides a cold source, a reboiler (112) of the first-stage alkane separation and purification tower provides a heat source, an outlet of each stage of condenser of the multi-stage alkane separation and purification tower is light hydrocarbon with different components, the light hydrocarbon enters a next-stage alkane separation and purification tower for further separation, an outlet of an m-stage alkane separation and purification tower is high-purity light hydrocarbon, and an outlet of the reboiler of each stage of alkane separation and purification tower is heavy hydrocarbon with different types;
s130, condensing high-purity light hydrocarbon from an outlet of a condenser (131) of the n-grade alkane separation and purification tower through a condenser (15), wherein the outlet of the condenser (15) is the high-purity light hydrocarbon of the product liquid.
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