CN108641769B - Recovery method of oilfield associated gas - Google Patents
Recovery method of oilfield associated gas Download PDFInfo
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- CN108641769B CN108641769B CN201810575982.5A CN201810575982A CN108641769B CN 108641769 B CN108641769 B CN 108641769B CN 201810575982 A CN201810575982 A CN 201810575982A CN 108641769 B CN108641769 B CN 108641769B
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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
- C10L3/12—Liquefied petroleum gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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Abstract
The invention provides a recovery method of oilfield associated gas, wherein a gas phase of a raw material after primary gas-liquid separation is compressed and cooled, then secondary gas-liquid separation and dehydration are carried out, a liquid phase after primary gas-liquid separation is subjected to flash evaporation, dehydration and steam stripping, and a gas phase obtained by steam stripping and a gas phase after flash evaporation are subjected to 2 times of compression and cooling and then enter a dehydration link; and (2) cooling the dehydrated and dried gas phase, then carrying out low-temperature gas-liquid separation, heating the liquid phase subjected to low-temperature separation, removing ethane, heating the liquid phase subjected to ethane removal, removing butane to obtain a liquid-phase LPG product, cooling part of liquid-phase condensate oil subjected to butane removal, and then taking the cooled part of liquid-phase condensate oil as an absorbent to carry out multi-stage mass transfer and heat transfer with the gas phase subjected to low-temperature separation in the liquefaction step, and cooling, low-temperature separation, pressure reduction and cold recovery on the gas phase subjected to mass transfer and heat transfer to obtain a lean gas. The method can recover the high-value LPG product in the associated gas of the oil field, and greatly reduces the production cost by adopting an efficient and economic process method.
Description
Technical Field
The invention belongs to the technical field of recovery and separation of oil field gas, and particularly relates to a recovery method of oil field associated gas.
Background
The traditional oil field gas recovery method adopts a high-pressure expansion refrigeration process or a DHX process.
The raw material gas in the high-pressure expansion refrigeration process is high-pressure (about 60 bar), low temperature is generated by utilizing Joule-Thomson throttling effect in the expansion process, and C in the raw material gas is condensed3、C4And (4) waiting for the heavy components. The DHX process adopts a propane ice machine for precooling and an expander for further refrigeration, wherein the deethanizer adopts the DHX process for further recovering C in the lean gas3、C4And (4) components.
Aiming at the pressure of raw material gas of about 20barg and C in the raw material gas3+C4The recovery of oil field gas with the content of about 19 percent (vt), the conveying pressure of lean gas of about 20barg and the outward conveying pressure of the lean gas basically consistent with the pressure of the raw material gas needs to use the raw material gas if the traditional high-pressure expansion refrigeration process is adoptedThe pressurization is carried out from 20barg to 60 barg, the pressurization power consumption is very high, and the follow-up pressurization equipment is high-pressure equipment and is not economical. If DHX process is used, C in raw material gas3The content is higher than 11 percent (vt), the excessive heavy hydrocarbon can cause the overhigh temperature at the top of the deethanizer, thus destroying the DHX process, and the DHX process has no obvious advantages. In addition, the recovery rate of LPG in the high-pressure expansion refrigeration process and the DHX process is not high, and is generally only about 80-90%.
Disclosure of Invention
In view of the above, the invention aims to provide a method for recovering associated gas in an oil field, which can recover a high-value LPG product in the associated gas in the oil field, and adopts an efficient and economic process method, so that the production cost is greatly reduced, and the recovery rate of the LPG reaches up to 99.8%.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a method for recovering oilfield associated gas comprises the following steps of: pressure-increasing separation, dehydration, liquefaction, refining and cold oil absorption;
the method comprises the following steps: pressure separation
The raw material is subjected to primary gas-liquid separation, a gas phase obtained after the primary gas-liquid separation is compressed and cooled and then subjected to secondary gas-liquid separation, the gas phase obtained after the secondary gas-liquid separation enters a dehydration link, a liquid phase obtained after the primary gas-liquid separation is subjected to flash evaporation, the liquid phase obtained after the flash evaporation is subjected to dehydration heating and then subjected to steam stripping, and the gas phase obtained after the steam stripping and the gas phase obtained after the flash evaporation enter the dehydration link after 2 times of compression and cooling;
step two: dewatering
Dehydrating and drying the gas phase subjected to the secondary gas-liquid separation;
step three: liquefaction
Carrying out low-temperature gas-liquid separation after the dehydrated and dried gas phase is cooled and partially liquefied, and carrying out cold energy recovery and temperature rise on the liquid phase after the low-temperature gas-liquid separation;
step four: refining
Removing light components such as ethane and the like from the liquid phase subjected to temperature rise in the third step, heating the liquid phase subjected to temperature rise and the like to remove butane, obtaining a liquid phase LPG product, cooling and cooling a part of condensate oil to be used as an absorbent, and performing the next step, wherein the rest condensate oil is used as a product to be extracted;
step five: cold oil absorption
Cooling the condensate oil, using the cooled condensate oil as an absorbent to perform multi-stage mass transfer and heat transfer with the gas phase subjected to low-temperature separation in the third step, recovering LPG components in the gas phase subjected to low-temperature separation in the third step,
and (3) cooling, low-temperature separation, pressure reduction and cold quantity recovery are carried out on the gas phase obtained after mass transfer and heat transfer, the gas phase is taken as lean gas to be extracted, and the liquid phase obtained after mass transfer and heat transfer is returned to the third step.
Further, the liquid phase after the second-stage gas-liquid separation is circulated back to be flashed.
Further, the gas phase after removing light components such as ethane is decompressed and recovered as lean gas to be extracted.
Further, in the first step, the raw gas enters a first-stage gas-liquid separator for gas-liquid separation, the liquid phase in the first-stage gas-liquid separator is subjected to LPG component recovery in the liquid phase through a flash tank, the liquid phase at the bottom of the flash tank is dehydrated through a decanter, the dehydrated oil phase is heated through a pump and a first-stage preheater and then enters a stripping tower for further recovery of LPG, the gas phase extracted from the top of the stripping tower and the gas phase at the top of the flash tank are pressurized through a first-stage compressor, the gas phase at the outlet of the first-stage compressor is cooled and enters the first-stage gas-liquid separator, and the gas phase passing through the top of the first.
Furthermore, the oil phase extracted from the bottom of the stripping tower is recovered by the waste heat of the primary preheater and then is stored in a condensate oil tank area, and the liquid phase of the secondary gas-liquid separator returns to the flash tank.
And further, the step two comprises a dehydration unit, a molecular sieve is arranged in the dehydration unit, a 4A molecular sieve is adopted, and the drying depth is required to be-40 ℃ of the dew point temperature of the gas.
And further, in the third step, the dried oil gas enters a cold box for partial condensation, then enters a downstream first-stage low-temperature gas-liquid separator for gas-liquid separation, the top gas phase of the first-stage low-temperature gas-liquid separator is sent to a downstream absorption tower for further recovery of LPG (liquefied petroleum gas) components in the gas phase, and the bottom liquid phase of the first-stage low-temperature gas-liquid separator enters a product refining unit for refining after cold energy is recovered by the cold box.
Further, in the fourth step, the removal of light components such as ethane and the like is carried out in a deethanizer, the oil phase at the bottom of the deethanizer is heated by a secondary heat exchanger and then enters a debutanizer, the qualified LPG product is at the top of the debutanizer, and the condensate oil component C is at the bottom of the debutanizer5 +。
And further, in the fifth step, after the condensate oil is subjected to heat exchange through a secondary heat exchanger, cooling and pump pressurization, a part of the condensate oil is used as an absorbent and enters an absorption tower of a cold oil absorption unit, a part of the condensate oil is used as a condensate oil product and is stored in a tank area, the absorbent is cooled and enters the top of the absorption tower, a gas phase from the top of the primary low-temperature gas-liquid separator enters the bottom of the absorption tower, the absorbent and the gas phase from the top of the primary low-temperature gas-liquid separator are in reverse contact in the absorption tower to perform multi-stage mass transfer and heat transfer and recover LPG components in the gas phase, and a liquid phase at the bottom of the absorption tower enters a deethanizer for circular refining after cold energy is.
Compared with the prior art, the recovery method of the oilfield associated gas has the following advantages:
1. the condensate generated by the raw material gas in the long-distance pipeline network process is recovered by adopting the processes of flash evaporation, decantation and a stripping tower, so that the yield of LPG can be improved on one hand, and the energy consumption for the subsequent molecular sieve dehydration can be reduced on the other hand;
2. the high-pressure booster is avoided, and the power consumption of the device and the equipment investment are reduced;
3. the refrigeration part adopts a pinch point technology, and a gas phase at the top of the primary low-temperature gas-liquid separator, a liquid phase at the bottom, a gas phase at the top of the deethanizer and cold oil circularly enter a cold box for cold energy recovery, so that the refrigeration capacity of the propane ice machine is reduced, and the consumption of the device is saved;
4. the refrigeration part adopts a cold box technology, so that the LPG loss caused by gas-liquid two phases generated during the graded refrigeration capacity recovery is avoided;
5. compared with the traditional hot oil absorption process, the process has the advantages that the process adopts the process of firstly pressurizing and cooling and then cooling oil absorption, and reduces the circulating dosage of a cooling oil absorbent, thereby reducing the energy consumption of the device;
6. the deethanizer adopts high-pressure separation, so that the refrigeration requirement on the tower top can be reduced, the lean gas output pressure on the tower top can be maintained, and a lean gas output compressor is avoided.
Drawings
Fig. 1 is a process flow diagram of oilfield associated gas recovery.
Description of reference numerals:
1-first-stage gas-liquid separator; 2-a flash tank; 3-a decanter; 5-primary preheater; 6-a stripping tower; 7-a first stage compressor; 9-a two-stage compressor; 11-a secondary gas-liquid separator; 12-a dehydration unit; 13-a cold box; 15-first-stage low-temperature gas-liquid separator; 16-a deethanizer; 17-a secondary heat exchanger; an 18-debutanizer column; 22-an absorption column; 24-two-stage low-temperature gas-liquid separator.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which the present invention belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following examples and FIG. 1.
The recovery method of the oilfield associated gas comprises the following steps: pressure-increasing separation, dehydration, liquefaction, refining and cold oil absorption:
the method comprises the following steps: pressure separation
The raw gas enters a first-stage gas-liquid separator 1 for gas-liquid separation, the liquid phase in the first-stage gas-liquid separator 1 is subjected to LPG component recovery in the liquid phase through a flash tank 2, the liquid phase at the bottom of the flash tank 2 is dehydrated through a decanter 3, the dehydrated oil phase is heated through a pump and a first-stage preheater 5 and then enters a stripping tower 6 for further recovery of LPG, and the butane content in the oil phase at the bottom of the stripping tower 6 is controlled within 0.3% (mole percentage).
The gas phase extracted from the top of the stripping tower 6 and the gas phase at the top of the flash tank 2 are pressurized to 20barg by a first-stage compressor 7, the gas phase at the outlet of the first-stage compressor 7 is cooled to enter a first-stage gas-liquid separator 1, the gas phase passing through the top of the first-stage gas-liquid separator 1 is pressurized to 31barg by a second-stage compressor 9, then is cooled to 45 ℃, enters a second-stage gas-liquid separator 11 for gas-liquid separation, the oil phase extracted from the bottom of the stripping tower 6 is recovered by the waste heat of a first-stage preheater 5 and then is stored in a condensate oil tank area, and the liquid phase of the.
Step two: dewatering
And (3) introducing the gas phase separated from the secondary gas-liquid separator 11 into a dehydration unit 12 for dehydration, wherein a molecular sieve is arranged in the dehydration unit 12, a 4A molecular sieve is adopted, and the drying depth is required to be-40 ℃ of the dew point temperature of the gas.
The main function is to remove the moisture of the raw material gas and avoid the icing phenomenon in the subsequent liquefaction.
Step three, liquefaction
The dried oil gas enters a cold box 13 for partial condensation, is cooled to-30 ℃, then enters a downstream first-stage low-temperature gas-liquid separator 15 for gas-liquid separation, the top gas phase of the first-stage low-temperature gas-liquid separator 15 is sent to a downstream absorption tower 22 for further recycling LPG (liquefied petroleum gas) components in the gas phase, and the bottom liquid phase of the first-stage low-temperature gas-liquid separator 15 enters a product refining unit for refining after cold energy is recycled by the cold box 13.
The main function is to reduce the temperature of the raw gas from the dehydration step, to condense most of the LPG component in the raw gas (while condensing, a small amount of light components will also be condensed into liquid phase) into liquid phase, which is then refined in the deethanizer 16 by cold recovery (temperature rise).
Step four, refining
The light components such as ethane and the like are removed in the deethanizer 16, the deethanizer 16 mainly has the function of separating the light components such as ethane and the like from C3, the top of the tower is used for gas phase extraction of the light components (C1+ C2), and the bottom of the tower is used for heavy component extraction (C3+ C4). The overhead pressure of the deethanizer 16 is controlled at 26barg with a reflux ratio of: 1.6. the oil phase at the bottom of the deethanizer 16 is heated by the secondary heat exchanger 17 and then enters the debutanizer 18, the debutanizer 18 mainly separates C4 and C5, LPG (C3+ C4) is extracted at the top of the tower, and condensate oil (more than C5 +) is extracted at the bottom of the tower. The overhead pressure of the debutanizer 18 was controlled at 11barg with a reflux ratio of: 1.2. the tower top of the debutanizer 18 is qualified LPG product, and the tower bottom is condensate oil component C5 +The gas phase extracted from the top of the deethanizer 16 is decompressed to 20barg by a J-T valve, and then recovered as lean gas by a cold box 13 after cold energy is recovered.
Step five, cold oil absorption
The condensate oil is subjected to heat exchange by the secondary heat exchanger 17, cooling and pump pressurization, one part of the condensate oil is used as an absorbent and enters the absorption tower 22, the other part of the condensate oil is used as a condensate oil product and is stored in a tank area, the absorbent is cooled to-30 ℃ and then enters the top of the absorption tower 22, a gas phase from the top of the primary low-temperature gas-liquid separator 15 enters the bottom of the absorption tower 22, and in the absorption tower 22, the absorbent and the gas phase from the top of the primary low-temperature gas-liquid separator 15 are in reverse contact, so that multi-stage mass transfer and heat transfer are performed, and LPG components in the gas phase are. The liquid phase at the bottom of the absorption tower 22 enters the deethanizer 16 for circular refining after cold energy is recovered by the cold box 13, the gas phase at the top of the absorption tower 22 is cooled to-30 ℃, condensate oil components in the gas phase are recovered, and the operation pressure of the absorption tower 22 is controlled at 30 barg.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (9)
1. A method for recovering oilfield associated gas is characterized by comprising the following steps: the raw materials sequentially pass through the following steps: pressure-increasing separation, dehydration, liquefaction, refining and cold oil absorption;
the method comprises the following steps: pressure separation
The raw material is subjected to primary gas-liquid separation, a gas phase obtained after the primary gas-liquid separation is compressed and cooled and then subjected to secondary gas-liquid separation, the gas phase obtained after the secondary gas-liquid separation enters a dehydration link, a liquid phase obtained after the primary gas-liquid separation is subjected to flash evaporation, the liquid phase obtained after the flash evaporation is subjected to dehydration heating and then subjected to steam stripping, and the gas phase obtained after the steam stripping and the gas phase obtained after the flash evaporation enter the dehydration link after 2 times of compression and cooling;
step two: dewatering
Dehydrating and drying the gas phase subjected to the secondary gas-liquid separation;
step three: liquefaction
Carrying out low-temperature gas-liquid separation after the dehydrated and dried gas phase is cooled and partially liquefied, and carrying out cold energy recovery and temperature rise on the liquid phase after the low-temperature gas-liquid separation;
step four: refining
Removing ethane light components from the liquid phase after heating in the third step, removing butane from the liquid phase after removing the ethane light components after heating, then obtaining a liquid phase LPG product, cooling and cooling the rest of the gas condensate to be used as an absorbent, and entering the next step, and extracting the rest of the gas condensate to be used as a product;
step five: cold oil absorption
Cooling the condensate oil, using the cooled condensate oil as an absorbent to perform multi-stage mass transfer and heat transfer with the gas phase subjected to low-temperature separation in the third step, recovering LPG components in the gas phase subjected to low-temperature separation in the third step,
and (3) cooling, low-temperature separation, pressure reduction and cold quantity recovery are carried out on the gas phase obtained after mass transfer and heat transfer, the gas phase is taken as lean gas to be extracted, and the liquid phase obtained after mass transfer and heat transfer is returned to the third step.
2. The method of recovering oilfield associated gas of claim 1, wherein: the liquid phase after the second-stage gas-liquid separation is circulated back for flash evaporation.
3. The method of recovering oilfield associated gas of claim 2, wherein: and decompressing the gas phase after removing the ethane light components, recovering cold energy, and extracting the gas phase as lean gas.
4. The method of recovering oilfield associated gas of claim 3, wherein: in the first step, raw gas enters a first-stage gas-liquid separator (1) for gas-liquid separation, a liquid phase in the first-stage gas-liquid separator (1) recovers an LPG component in the liquid phase through a flash tank (2), a liquid phase at the bottom of the flash tank (2) is dehydrated through a decanter (3), a dehydrated oil phase is heated through a pump and a first-stage preheater (5) and then enters a stripping tower (6) for further recovering LPG, a gas phase extracted from the top of the stripping tower (6) and a gas phase at the top of the flash tank (2) are pressurized through a first-stage compressor (7), a gas phase at an outlet of the first-stage compressor (7) is cooled and enters the first-stage gas-liquid separator (1), a gas phase passing through the top of the first-stage gas-liquid separator (1) is pressurized through a second-.
5. The method of recovering oilfield associated gas of claim 4, wherein: and the oil phase at the bottom of the stripping tower (6) is recovered from the waste heat of the primary preheater (5) and then is stored in a condensate tank area, and the liquid phase of the secondary gas-liquid separator (11) returns to the flash tank (2).
6. The method of recovering oilfield associated gas of claim 3, wherein: the second step comprises a dehydration unit (12), a molecular sieve is arranged in a dehydration tank, a 4A molecular sieve is adopted, and the drying depth is required to be-40 ℃ of the dew point temperature of the gas.
7. The method of recovering oilfield associated gas of claim 3, wherein: in the third step, the dried oil gas enters a cold box (13) for partial condensation, then enters a downstream first-stage low-temperature gas-liquid separator (15) for gas-liquid separation, the top gas phase of the first-stage low-temperature gas-liquid separator (15) enters a downstream absorption tower (22) for further recycling LPG (liquefied petroleum gas) components in the gas phase, and the bottom liquid phase of the first-stage low-temperature gas-liquid separator (15) enters a product refining unit for refining after cold energy is recycled by the cold box (13).
8. The method of recovering oilfield associated gas of claim 3, wherein: in the fourth step, the removal of ethane light components is carried out in a deethanizer (16), the oil phase at the bottom of the deethanizer (16) is heated by a secondary heat exchanger (17) and then enters a debutanizer (18), the top of the debutanizer (18) is a qualified LPG product, and the bottom of the debutanizer is a condensate oil component C5 +。
9. The method of recovering oilfield associated gas of claim 3, wherein: in the fifth step, condensate oil is subjected to heat exchange through a secondary heat exchanger (17), is cooled and is pressurized by a pump, a part of condensate oil is used as an absorbent to enter an absorption tower (22) of a cold oil absorption unit, a part of condensate oil is used as a condensate oil product to be stored in a tank area, the absorbent is cooled and enters the top of the absorption tower (22), a gas phase from the top of a primary low-temperature gas-liquid separator (15) enters the bottom of the absorption tower (22), the absorbent is in reverse contact with the gas phase from the top of the primary low-temperature gas-liquid separator (15) in the absorption tower (22) to carry out multi-stage mass transfer and heat transfer, an LPG component in the gas phase is recovered, and a liquid phase at the bottom of the absorption tower (22) enters a deethanizer (16) to be subjected to cyclic refining after cold energy is recovered.
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| CN111717915B (en) * | 2019-03-19 | 2022-02-01 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
| CN110093197B (en) * | 2019-05-23 | 2024-04-26 | 中国石油化工股份有限公司 | Denitrification method and denitrification system for oilfield associated gas |
| CN111004657B (en) * | 2019-12-11 | 2021-04-27 | 中国天辰工程有限公司 | Method for comprehensively utilizing oilfield associated gas |
| CN112980489B (en) * | 2019-12-16 | 2023-08-08 | 天津深蓝化工技术有限公司 | Process method for recycling light hydrocarbons of associated gas of open refrigeration oilfield |
| CN112745974B (en) * | 2020-12-14 | 2021-07-06 | 中海石油(中国)有限公司 | Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment |
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