CN111456702A - Oil-gas separation system and method - Google Patents
Oil-gas separation system and method Download PDFInfo
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- CN111456702A CN111456702A CN201910047809.2A CN201910047809A CN111456702A CN 111456702 A CN111456702 A CN 111456702A CN 201910047809 A CN201910047809 A CN 201910047809A CN 111456702 A CN111456702 A CN 111456702A
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- 238000000926 separation method Methods 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 229
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 182
- 239000002994 raw material Substances 0.000 claims abstract description 103
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 97
- 239000003345 natural gas Substances 0.000 claims abstract description 91
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 86
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 42
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 42
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 40
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims description 39
- 239000000203 mixture Substances 0.000 claims description 25
- 238000007710 freezing Methods 0.000 claims description 13
- 230000008014 freezing Effects 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 3
- 238000013461 design Methods 0.000 abstract description 4
- 239000003570 air Substances 0.000 description 89
- 229920006395 saturated elastomer Polymers 0.000 description 11
- 230000000903 blocking effect Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 5
- 208000005156 Dehydration Diseases 0.000 description 4
- 230000020335 dealkylation Effects 0.000 description 4
- 238000006900 dealkylation reaction Methods 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 206010060904 Freezing phenomenon Diseases 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229920001021 polysulfide Polymers 0.000 description 1
- 239000005077 polysulfide Substances 0.000 description 1
- 150000008117 polysulfides Polymers 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 229930192474 thiophene Natural products 0.000 description 1
- 150000003577 thiophenes Chemical class 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
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- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention provides an oil-gas separation system and a method, belonging to the technical field of oil-gas separation, wherein the oil-gas separation system comprises a gas-liquid separator, an air cooler, a water separator, a precooler, a throttle expansion valve, a low-temperature separator and an ethylene glycol conveying pipeline; the precooler comprises a cold air flow channel and a hot air flow channel which are mutually isolated and can exchange heat; the gas-liquid separator, the air cooler, the water separator, the cold air runner, the throttle expansion valve and the low-temperature separator are sequentially connected in series, the gas inlet of the gas-liquid separator is connected with the raw material gas inlet pipe, the gas outlet of the low-temperature separator is connected with the gas inlet of the cold air runner, and the gas outlet of the cold air runner is communicated with the natural gas output pipeline; the glycol conveying pipeline is communicated with the water separator. The oil-gas separation system and the method provided by the invention enable the existing ethylene glycol filling amount to meet the requirement that the throttle expansion valve operates under the design condition, can prevent the low-temperature separator and the throttle expansion valve from being frozen and blocked, and improve the yield of natural gas and light hydrocarbon.
Description
Technical Field
The invention relates to the technical field of oil-gas separation, in particular to an oil-gas separation system and method.
Background
In the oil gas exploitation, contain a large amount of moisture, light hydrocarbon mixture and heavy hydrocarbon mixture etc. in the feed gas, need carry out dehydration and dealkylation to the feed gas and handle, promote the quality and the natural gas and the light hydrocarbon output of natural gas.
At present, the raw material gas is dehydrated and dealkylated by adopting a throttle expansion valve throttling refrigeration and ethylene glycol anti-freezing process, and the quality of the exported natural gas and the yield of the natural gas and light hydrocarbon are determined by the refrigeration temperature of the throttle expansion valve and the separation effect of a low-temperature separator.
The temperature and the moisture content of the raw material gas which can be processed by the existing oil-gas separation system are lower than those of the actual raw material gas to be processed, so that the existing ethylene glycol filling amount cannot meet the requirement that the throttle expansion valve operates under the design condition, the low-temperature separator and the throttle expansion valve are frequently frozen and blocked, and the yield of natural gas and light hydrocarbon is reduced.
Disclosure of Invention
The invention provides an oil-gas separation system and method, which can prevent a low-temperature separator and a throttle expansion valve from being frozen and blocked and improve the yield of natural gas and light hydrocarbon.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides an oil-gas separation system, which comprises a gas-liquid separator, an air cooler, a water separator, a precooler, a throttle expansion valve, a low-temperature separator and an ethylene glycol conveying pipeline, wherein the gas-liquid separator is arranged on the upper part of the air cooler; the precooler comprises a cold air runner and a hot air runner which are isolated from each other and can exchange heat; the gas-liquid separator, the air cooler, the water separator, the cold airflow channel, the throttle expansion valve and the low-temperature separator are sequentially connected in series, an air inlet of the gas-liquid separator is connected with a raw material air inlet pipe, an air outlet of the low-temperature separator is connected with an air inlet of the cold airflow channel, and an air outlet of the cold airflow channel is communicated with a natural gas output pipeline; the ethylene glycol conveying pipeline is communicated with the hot air channel.
Further, the low-temperature separator is connected with the cold air runner through a first pipeline;
a temperature control valve is arranged between the first pipeline and the natural gas output pipeline, and divides the dry and cold natural gas from the low-temperature separator into two paths, wherein one path flows to the cold gas flow channel, and the other path flows to the natural gas output pipeline.
Further, the oil-gas separation system also comprises a temperature sensor and a control device; the temperature sensor is arranged in the natural gas output pipeline and used for detecting the temperature of the natural gas; the control device is respectively in signal connection with the temperature sensor and the temperature control valve, and the target temperature of the natural gas is preset in the control device; and the control device receives the temperature collected by the temperature sensor, compares the temperature with the target temperature of the natural gas and controls the opening of the temperature control valve.
Further, the oil-gas separation system also comprises a slug flow catcher; the slug flow catcher is arranged on the raw material inlet pipe connected with the air inlet of the gas-liquid separator and is used for pre-separating raw material gas.
Further, the air cooler comprises a shell, and a cooling pipe and a cooling fan which are arranged in the shell; the cooling pipe is used for introducing a feed gas to be cooled; the cooling fan provides cooling air for cooling the cooling pipe.
Further, a swirler is arranged at an air inlet of the water separator; the air inlet of the water separator is sequentially provided with a net pad and a fog pad on a flow path from the air inlet to the air outlet of the water separator, and the fog pad is close to the air outlet of the water separator.
Further, the oil-gas separation system also comprises a condensate oil treatment device; the gas-liquid separator, the water separator and the low-temperature separator are all provided with liquid discharge ports, and the liquid discharge ports are communicated with the condensate oil treatment device through second pipelines.
In another aspect, the invention provides an oil-gas separation method, which comprises the following steps:
s100, feeding the raw material gas into a gas-liquid separator to separate part of heavy hydrocarbon mixture and condensate water from the raw material gas;
s200, feeding the raw material gas separated by the gas-liquid separator into an air cooler for cooling, so that the raw material gas is cooled from a first temperature to a second temperature;
step S300, feeding the raw material gas cooled by the air cooler into a water separator to separate part of light hydrocarbon mixture and condensate water from the raw material gas;
s400, feeding the raw material gas separated by the water separator into a hot gas flow passage of a precooler, and performing heat exchange with dry and cold natural gas separated by a low-temperature separator to reduce the temperature of the raw material gas to a third temperature; injecting glycol into the hot gas flow channel, and fully mixing the glycol with the raw material gas to reduce the freezing point of the condensed water;
step S500, the raw material gas after heat exchange enters a throttling expansion valve, so that the temperature of the raw material gas is reduced from a third temperature to a fourth temperature, and the pressure is reduced from a first pressure to a second pressure;
step S600; the raw gas after passing through the throttle expansion valve enters a low-temperature separator, and the raw gas is cooled and depressurized in the low-temperature separator, so that part of light hydrocarbon mixture, condensate water and glycol are separated from the raw gas.
Further, before step S100, the moisture of the raw material gas may be primarily separated.
Further, in step S400, the flow rate of the dry and cold natural gas flowing into the precooler is adjusted by the temperature control valve, so as to control the temperature and moisture of the raw gas flowing into the throttle expansion valve.
Compared with the prior art, the oil-gas separation system and the method provided by the invention have the following advantages;
the oil-gas separation system and the method provided by the invention have the advantages that the air cooler and the water separator are arranged between the gas-liquid separator and the precooler, the raw material gas is dehydrated and processed at low temperature before entering the precooler, the moisture of the raw material gas entering the precooler can be reduced, the consumption of ethylene glycol can be further reduced, the existing ethylene glycol filling amount can meet the requirement that a throttle expansion valve operates under the design condition, the low-temperature separator and the throttle expansion valve can be prevented from being frozen and blocked, and the yield of natural gas and light hydrocarbon is improved.
In addition to the technical problems solved by the present invention, the technical features constituting the technical solutions, and the advantages brought by the technical features of the technical solutions described above, other technical problems solved by the present invention, other technical features included in the technical solutions, and advantages brought by the technical features will be further described in detail in the detailed description of the present invention.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments of the present invention or the prior art will be briefly described below, it is obvious that the drawings in the following description are only a part of the embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic diagram I of the structure of an oil-gas separation system provided by the embodiment of the invention;
FIG. 2 is a schematic structural diagram II of an oil-gas separation system provided in the embodiment of the present invention;
FIG. 3 is a schematic diagram of the connection between a control device and a temperature control valve and a temperature sensor according to an embodiment of the present invention;
FIG. 4 is a first schematic diagram illustrating the steps of a first oil-gas separation method according to an embodiment of the present invention;
FIG. 5 is a schematic diagram of the second step of the oil-gas separation method according to the embodiment of the present invention.
Description of reference numerals:
10-a gas-liquid separator, wherein,
20-an air cooler is arranged at the lower part of the air cooler,
30-a water separator is arranged at the bottom of the water tank,
40-a pre-cooler is arranged in the pre-cooler,
50-a throttle expansion valve, wherein the throttle expansion valve is arranged on the upper portion of the shell,
60-a low-temperature separator, wherein,
70-a temperature-controlled valve is arranged in the vacuum chamber,
an 80-ethylene glycol delivery line,
90-a raw material inlet pipe, wherein,
100-a condensate treatment device, wherein the condensate treatment device comprises a condensate treatment device,
101-the first line-up of the first line,
102-the second line-up of the second line,
103-a natural gas output pipeline,
104-a slug flow catcher,
105-a temperature sensor-the temperature of the sample,
106-control means.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. It is to be understood that the described embodiments are merely a few embodiments of the invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in fig. 1, the oil-gas separation system provided in the embodiment of the present invention includes a gas-liquid separator 10, an air cooler 20, a water separator 30, a precooler 40, a throttle expansion valve 50, a low-temperature separator 60, and a glycol conveying pipeline 80; the precooler 40 comprises a cold air flow channel and a hot air flow channel which are isolated from each other and can exchange heat; the gas-liquid separator 10, the air cooler 20, the water separator 30, the cold air runner, the throttle expansion valve 50 and the low-temperature separator 60 are sequentially connected in series, the air inlet of the gas-liquid separator 10 is connected with the raw material air inlet pipe 90, the air outlet of the low-temperature separator 60 is connected with the air inlet of the cold air runner, and the air outlet of the cold air runner is communicated with the natural gas output pipeline 103; the glycol delivery line 80 is in communication with the hot gas flow path.
Specifically, the raw gas collected from the oil-gas well has the characteristics of high temperature, high pressure and high water content, does not accord with the quality of commercial natural gas, and needs to be dehydrated and dehydrogenated. At present, an oil-gas separation system is usually adopted to carry out dehydration and dealkylation treatment on feed gas, so that moisture, heavy hydrocarbon mixture and light hydrocarbon mixture in the feed gas are separated from the feed gas, and the dry and cold natural gas which meets the output quality of the natural gas is obtained.
The oil-gas separation system comprises a gas-liquid separator 10, the gas-liquid separator 10 is used for carrying out primary separation on the raw material gas, the gas inlet of the gas-liquid separator 10 is connected with a raw material inlet pipe 90, and the gas outlet of the gas-liquid separator 10 is connected with the gas inlet of an air cooler 20.
Natural gas and condensate oil (the condensate oil refers to a liquid phase component condensed from a condensate gas field or oil field associated natural gas, the main component of the condensate oil is a mixture of C5-C11 + hydrocarbons, and the condensate oil contains a small amount of hydrocarbons larger than C8 and impurities such as sulfur dioxide, thiophenes, thiols, thioether and polysulfide, and the heavy hydrocarbon mixture and the light hydrocarbon mixture are gradually separated from raw gas along with the gradual reduction of temperature and pressure) from the bottom of a well are conveyed to an oil-gas treatment system arranged in an oil-gas treatment plant through a gas collecting main line for carrying out the dealkylation and dehydration treatment, and is conveyed into a raw material inlet pipe 90 of the oil gas treatment system, after being buffered and primarily separated by a gas-liquid separator 10, impurities, part of water and condensate oil (mainly heavy hydrocarbon mixture) in the feed gas are separated out, and the feed gas subjected to primary separation by the gas-liquid separator 10 is conveyed to the air cooler 20.
The air cooler 20 is also called an air cooler, and the air cooler 20 is a device that cools or condenses the high-temperature fluid flowing through the air cooler 20 by using ambient air as a cooling medium. In this embodiment, the air inlet of the air cooler 20 is connected to the air outlet of the gas-liquid separator 10, the air outlet of the air cooler 20 is connected to the air inlet of the water separator 30, and the air outlet of the water separator 30 is connected to the air inlet of the precooler 40. The raw material gas after the first-stage separation by the gas-liquid separator 10 enters the air cooler 20 to be cooled, so that the temperature of the raw material gas is reduced, and gaseous water contained in the raw material gas is more easily separated out along with the reduction of the temperature of the raw material gas. The raw material gas cooled by the air cooler 20 enters the water separator 30 for secondary separation, and most of gaseous water and condensate oil (part of light hydrocarbon mixture) of the raw material gas are separated out by the water separator 30. .
The precooler 40 comprises a hot air flow channel and a cold air flow channel which are isolated from each other and can exchange heat; one end of the hot air channel is connected with the air outlet of the water separator 30, and the other end is communicated with the throttle expansion valve 50; the cold gas flow channel is connected with the gas outlet of the low-temperature separator 60, namely the hot gas flow channel introduces the raw gas, the cold gas flow channel introduces the dry and cold natural gas, and the temperature of the dry and cold natural gas in the cold gas flow channel is lower than the temperature of the raw gas of the hot gas flow channel; after the heat exchange between the raw gas and the dry-cooled natural gas occurs, the temperature of the raw gas is further reduced, and the temperature of the dry-cooled natural gas is increased, so that the temperature requirement of the output natural gas can be met.
In order to prevent the separated liquid water in the raw material gas from causing freezing and blocking phenomena to the throttle expansion valve 50 and the low-temperature separator 60 in a low-temperature environment, a glycol conveying pipeline can be connected to an air inlet of the precooler 40 to mix the glycol with the raw material gas, the glycol is mixed with the separated water to form a glycol solution, the freezing point of the glycol solution is low, and the freezing phenomenon cannot occur when the raw material gas enters the throttle expansion valve 50. In this embodiment, the ethylene glycol is injected into the precooler 40 before the raw material gas exchanges heat with the dry-cooled natural gas, so that the liquid water separated out from the raw material gas in the heat exchange process can be prevented from freezing and blocking the precooler 40, and the throttle expansion valve 50 and the low-temperature separator 60 can be prevented from freezing and blocking.
The air inlet of the throttle expansion valve 50 is connected with the air outlet of the precooler 40, and the air outlet of the throttle expansion valve 50 is connected with the air inlet of the low-temperature separator 60; the expansion valve 50 expands the gas by throttling and decompressing to generate a low temperature, in this embodiment, a J-T valve (the J-T valve is a joule-thomson expansion valve, and a throttle valve designed by utilizing the joule-thomson throttling expansion principle) is preferably adopted, the temperature and the pressure of the raw material gas are further reduced after passing through the expansion valve 50, the raw material gas after being cooled and decompressed by the expansion valve 50 enters a low-temperature separator 60, the raw material gas entering the low-temperature separator 60 forms dry and cold natural gas, condensate oil (light hydrocarbon mixture) and liquid water, the condensate oil enters a light hydrocarbon recovery device to be separated to obtain ethylene glycol barren solution and hydrocarbon liquid, the hydrocarbon liquid is further separated into light hydrocarbon and liquefied gas products, and the ethylene glycol barren solution enters an ethylene glycol regeneration device to be reused; the dry and cold natural gas from the low-temperature separator 60 exchanges heat with the raw material gas, and is output after the temperature is raised to a certain temperature.
It is understood that the oil-gas separation system in this embodiment further includes a condensate treatment device 100; the gas-liquid separator 10, the water separator 30, and the low-temperature separator 60 are each provided with a liquid discharge port, and the liquid discharge ports are communicated with the condensate treatment apparatus 100 through a second pipeline 102. Specifically, the bottoms of the gas-liquid separator 10, the water separator 30 and the low-temperature separator 60 are all provided with liquid discharge ports, the liquid discharge ports are all communicated through a second pipeline 102, and the other end of the second pipeline 102 is communicated with the condensate oil treatment device 100; the condensate and the condensate water separated out by the separator, the water separator 30 and the low-temperature separator 60 are conveyed into the condensate treatment device 100 through a liquid outlet and a second pipeline 102, and the condensate is further separated into stable light hydrocarbon and liquefied gas products by the condensate treatment device 100.
According to the oil-liquid separation system provided by the invention, the air cooler 20 and the water separator 30 are arranged between the precooler 40 and the gas-liquid separator 10, so that part of water vapor in the feed gas can be separated out, the water content in the feed gas flowing into the precooler 40 is reduced, the usage amount of ethylene glycol is reduced, the conventional ethylene glycol filling amount can meet the requirement that the throttle expansion valve 50 operates under the design condition, the low-temperature separator 60 and the throttle expansion valve 50 can be prevented from being frozen and blocked, and the yield of natural gas and light hydrocarbon is improved.
In this embodiment, the low temperature separator 60 is connected to the cold air flow passage through a first pipeline 101; a temperature control valve 70 is arranged between the first pipeline 101 and the natural gas output pipeline 103, and the temperature control valve 70 divides the dry and cold natural gas from the low-temperature separator 60 into two paths, wherein one path flows to the cold gas flow channel, and the other path flows to the natural gas output pipeline 103.
Specifically, the air outlet of the low-temperature separator 60 is connected to the cold air channel through the first pipeline 101, so that the dry and cold natural gas separated by the low-temperature separator 60 can be conveyed into the cold air channel of the precooler 40, and the dry and cold natural gas exchanges heat with the raw material gas passing through the hot air channel of the precooler 40, so as to raise the output temperature of the dry and cold natural gas and lower the temperature of the raw material gas flowing to the throttle expansion valve 50.
The dry and cold natural gas after heat exchange is conveyed to the natural gas output pipeline 103, in order to conveniently adjust the temperature of the natural gas in the natural gas output pipeline 103, a temperature control valve 70 is arranged between the first pipeline 101 and the natural gas output pipeline 103, the dry and cold natural gas flowing out of the low-temperature separator 60 can be divided into two paths by the temperature control valve 70, wherein one path flows into a cold gas flow channel of the precooler 40, and is conveyed to the natural gas output pipeline 103 after heat exchange with the raw gas; the other path does not exchange heat with the raw gas and can directly flow into the natural gas output pipeline 103 to adjust the temperature of the natural gas in the natural gas output pipeline 103. For example, when the temperature of the natural gas flowing out of the precooler 40 exceeds the temperature of the preset natural gas to be transported, the thermostatic valve 70 may be opened to allow part of the dry and cold natural gas to directly flow into the natural gas output pipeline 103, so as to regulate the temperature of the natural gas in the natural gas output pipeline 103.
As shown in fig. 3, further, in order to realize the automatic adjustment of the opening degree of the thermo valve 70, the oil-gas separation system provided in this embodiment further includes a temperature sensor 105 and a control device 106; the temperature sensor 105 is disposed in the natural gas output pipeline 103, the control device 106 may be disposed at a remote location (e.g., a monitoring platform), a signal input of the control device 106 is connected to the temperature sensor 103, and a signal output of the control device 106 is connected to the thermostatic valve 70. Wherein, the control device 106 is preset with the corresponding relation between the target temperature and the corresponding temperature difference of the exported natural gas and the opening degree of the temperature control valve 70; the temperature sensor 105 is configured to monitor the temperature of the exported natural gas in real time, transmit the acquired temperature data to the control device 106, and the control device 106 receives the temperature of the natural gas, compares the temperature with a preset target temperature of the exported natural gas, generates a command for controlling the opening of the temperature control valve 70, and transmits the command to the temperature control valve 70. If the real-time monitored natural gas temperature is higher than the preset target natural gas temperature, the opening of the corresponding temperature control valve 70 is increased, otherwise, the opening of the temperature control valve 70 is decreased. In the embodiment, the temperature sensor is arranged in the natural gas output pipeline 103, the control device can be arranged at a far end (such as a monitoring platform), the temperature of the exported natural gas can be adjusted in real time, and the quality of the exported natural gas is improved.
As shown in fig. 2, in the present embodiment, a slug flow catcher 104 is further disposed in the oil-gas separation system, the slug flow catcher 104 is connected to the raw material inlet pipe 90, and an air outlet of the slug flow catcher 104 is connected to an air inlet of the gas-liquid separator 10, the slug flow catcher 104 pre-separates the raw material gas flowing into the gas-liquid separator 10, so as to separate out impurities and partial saturated water in the raw material gas, and improve the oil-liquid separation efficiency and the water content in the raw material gas.
In this embodiment, the air cooler 20 includes a housing, and a cooling pipe and a cooling fan disposed in the housing; the cooling pipe is used for introducing a raw material gas to be cooled; the cooling fan provides cooling air for cooling the cooling pipe. Specifically, the air cooler 20 includes a housing, a cooling cavity is disposed in the housing, a cooling tube and a plurality of cooling fans are disposed in the cooling cavity, and the raw material gas is introduced from one end of the cooling tube, is led out from the other end of the cooling tube, and is connected to the hot flow path of the precooler 40 through a pipeline. After the raw material gas enters the cooling pipe, cooling air provided by the cooling fan blows the surface of the cooling pipe to cool the raw material gas in the cooling pipe. It can be understood that, in order to enhance the heat dissipation effect of the air cooler 20, the cooling pipe may be spirally disposed in the casing, so as to increase the flow path of the raw material gas in the air cooler 20, and enhance the cooling effect on the raw material gas.
The water separator 30 provided in this embodiment is provided with a swirler at an air inlet thereof; a gauze pad and a mist pad are sequentially arranged on a flow path from the air inlet of the water separator 30 to the air outlet thereof, and the mist pad is arranged close to the air outlet of the water separator 30. Specifically, the gas inlet of the water separator 30 is provided with a cyclone, and a stainless steel pipe with a longitudinal slit is arranged on the pipe wall, so that liquid is separated by centrifugal force to perform primary gas-liquid separation; the air current upwards in-process through the silk screen pad with the moisture in the separation of condensing, gas continues the ascending, through second grade fog pad, carries out secondary gas defoaming to further improve gas-liquid separation's efficiency, the qualified dry gas of separation gets into precooler 40 and carries out the heat transfer.
As shown in fig. 4, another aspect of the embodiment of the present invention provides an oil-gas separation method, which uses the oil-gas separation system to perform a dehydration and dealkylation process, specifically including the following steps;
step S100, the raw gas enters a gas-liquid separator 10 of a gas-liquid separator, so that part of heavy hydrocarbon mixture and condensate water are separated from the raw gas. Specifically, the raw material gas from the raw material gas inlet pipe 90 enters the gas-liquid separator 10 to perform first-stage separation, a hydrocarbon mixture and saturated water in the raw material gas are separated out from the raw material gas, the saturated water flows from a liquid outlet at the bottom of the gas-liquid separator 10 to the second pipeline 102 along with condensate (heavy hydrocarbon mixture), the saturated water is conveyed to the condensate treatment device 100 of the condensate treatment device through the second pipeline 102, and the condensate treatment device 100 of the condensate treatment device further decomposes and treats the condensate to obtain stable light hydrocarbon and liquefied gas products.
And step S200, the raw material gas separated by the gas-liquid separator 10 enters the air cooler 20 for cooling, so that the raw material gas is cooled from the first temperature to the second temperature. Specifically, the raw material gas primarily separated by the gas-liquid separator 10 enters the air cooler 20, the air cooler 20 cools the raw material gas to reduce the temperature of the raw material gas from a first temperature to a second temperature, and the cooled raw material gas enters the water separator 30. In this embodiment, the feed gas passing through the air cooler 20 may be cooled from 65 ℃ to 40 ℃.
Step S300, the raw material gas cooled by the air cooler 20 enters the water separator 30, so that part of light hydrocarbon mixture and condensed water are separated from the raw material gas. Specifically, the raw material gas cooled by the air cooler 20 enters the water separator 30, the water separator 30 performs secondary separation on the raw material gas, as the temperature of the raw material gas decreases, part of saturated water and light hydrocarbon mixture is separated out from the raw material gas in the water separator 30, the separated saturated water is discharged to the second pipeline 102 from a liquid discharge port located at the bottom of the water separator 30 along with condensate oil (light hydrocarbon mixture), and is conveyed to the condensate oil processing device 100 through the second pipeline 102, and the condensate oil processing device 100 decomposes the light hydrocarbon mixture into stable light hydrocarbon and liquefied gas products.
The temperature and water content of the raw material gas passing through the air cooler 20 and the water separator 30 are reduced, and the raw material gas is conveyed to the precooler 40 for further cooling.
Step S400, the raw material gas separated by the water separator 30 enters a hot gas flow passage of the precooler 40 and exchanges heat with the dry and cold natural gas separated by the low-temperature separator 60 to reduce the temperature of the raw material gas to a third temperature; and (3) injecting the ethylene glycol into the hot air runner, and fully mixing the ethylene glycol with the raw material gas to reduce the freezing point of the condensed water. Specifically, the raw material gas that is subjected to the secondary separation by the water separator 30 enters the hot gas channel of the precooler 40, and since the temperature of the dry and cold natural gas that flows in from the cooler channel of the precooler 40 is lower than the temperature of the raw material gas in the hot gas channel, the raw material gas can perform heat exchange with the dry and cold natural gas, so that the temperature of the raw material gas that flows through the hot gas channel is further reduced, that is, the temperature of the raw material gas is reduced from the second temperature to the third temperature, in this embodiment, the temperature of the raw material gas after heat exchange in the hot gas channel can be reduced from 40 ℃ to-. The temperature of the dry, cold natural gas flowing through the cold gas flow path after heat exchange is raised to 25 ℃.
In order to prevent the saturated water separated from the cooled raw material gas from causing the freezing and blocking phenomena on the throttling expansion valve 50, before the raw material gas flows into the precooler 40, the ethylene glycol can be introduced, the ethylene glycol and the saturated water are mixed to form an ethylene glycol solution which can reduce the freezing point of the water, and the freezing and blocking phenomena caused by the further cooling of the raw material gas in the throttling expansion valve 50 can be effectively prevented.
Step S500, the heat-exchanged raw material gas enters the throttle expansion valve 50, so that the temperature of the raw material gas is reduced from the third temperature to the fourth temperature, and the pressure is reduced from the first pressure to the second pressure. Specifically, the raw material gas flowing through the hot gas flow channel flows into the throttle expansion valve 50, and the throttle expansion valve 50 reduces the pressure and the temperature of the raw material gas to a fourth temperature from a third temperature, and the pressure is reduced from the first pressure to a second pressure, so that the temperature of the raw material gas can be reduced from-5 ℃ to-20 ℃ and the pressure is reduced to 6.5-7.1MPa under the action of the throttle expansion valve 50.
Step S600; the raw gas after passing through the throttle expansion valve 50 enters the low-temperature separator 60, and the raw gas is further cooled and depressurized in the low-temperature separator 60, so that part of light hydrocarbon mixture, condensate water and glycol are separated from the raw gas. Specifically, the raw gas passing through the throttle expansion valve 50 enters the low-temperature separator 60, the low-temperature separator 60 performs three-stage separation on the raw gas, and the raw gas is further separated in the low-temperature separator 60, so that a light hydrocarbon mixture, saturated water and ethylene glycol are separated out from the raw gas, and dry and cold natural gas is obtained. The condensate water flows from the drain port of the low-temperature separator 60 to the second pipeline 102 along with the condensate oil, and is conveyed to the condensate oil treatment device 100 through the second pipeline 102; the condensate treatment device 100 further decomposes the condensate to produce stable light hydrocarbon and liquefied gas products; the dry and cold natural gas separated by the low-temperature separator 60 is conveyed into the cold gas flow passage through the first pipeline 101, the feed gas in the precooler 40 is cooled, and the temperature of the dry and cold natural gas is raised, so that the quality of the exported natural gas is met.
As shown in fig. 5, before step S100, the moisture of the raw material gas may be primarily separated. Specifically, the saturated water in the raw gas entering the gas-liquid separator 10 is primarily separated; simultaneously, also can separate the impurity in the feed gas, can promote the quality of the dry and cold natural gas and the light hydrocarbon of being separated by the feed gas.
In this embodiment, in step S400, the flow rate of the dry and cold natural gas flowing into the precooler 40 is adjusted by the temperature control valve 70, so as to control the temperature and moisture of the raw gas flowing into the throttle expansion valve 50. Specifically, the temperature control valve 70 is arranged between the first pipeline 101 and the natural gas output pipeline 103, the temperature control valve 70 can divide the dry and cold natural gas flowing out from the low-temperature separator 60 into two paths, wherein one path flows into the cold gas flow path of the precooler 40, and is conveyed into the natural gas output pipeline 103 after exchanging heat with the raw gas, when the temperature of the raw gas flowing through the throttle expansion valve 50 is too low, and more saturated water is separated out, so that the danger of freezing and blocking of the throttle expansion valve 50 exists, the input amount of the dry and cold natural gas in the cold gas flow path of the precooler 40 can be reduced, the heat exchange of the raw gas is weakened, and the freezing and blocking of the throttle expansion valve 50 caused by too low temperature of the raw.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. An oil-gas separation system is characterized by comprising a gas-liquid separator, an air cooler, a water separator, a precooler, a throttle expansion valve, a low-temperature separator and an ethylene glycol conveying pipeline;
the precooler comprises a cold air runner and a hot air runner which are isolated from each other and can exchange heat;
the gas-liquid separator, the air cooler, the water separator, the cold airflow channel, the throttle expansion valve and the low-temperature separator are sequentially connected in series, an air inlet of the gas-liquid separator is connected with a raw material air inlet pipe, an air outlet of the low-temperature separator is connected with an air inlet of the cold airflow channel, and an air outlet of the cold airflow channel is communicated with a natural gas output pipeline;
the ethylene glycol conveying pipeline is communicated with the hot air channel.
2. The oil and gas separation system of claim 1, wherein the cryogenic separator is connected to the cold gas flowpath by a first conduit;
a temperature control valve is arranged between the first pipeline and the natural gas output pipeline, and divides the dry and cold natural gas from the low-temperature separator into two paths, wherein one path flows to the cold gas flow channel, and the other path flows to the natural gas output pipeline.
3. The oil and gas separation system of claim 2, further comprising a temperature sensor and a control device;
the temperature sensor is arranged in the natural gas output pipeline and used for detecting the temperature of the natural gas;
the control device is respectively in signal connection with the temperature sensor and the temperature control valve, and the target temperature of the natural gas is preset in the control device;
and the control device receives the temperature collected by the temperature sensor, compares the temperature with the target temperature of the natural gas and controls the opening of the temperature control valve.
4. The oil and gas separation system of claim 1, further comprising a slug flow trap;
the slug flow catcher is arranged on the raw material inlet pipe connected with the air inlet of the gas-liquid separator and is used for pre-separating raw material gas.
5. The oil-gas separation system of claim 1, wherein the air cooler comprises a housing and a cooling tube and a cooling fan disposed within the housing;
the cooling pipe is used for introducing a feed gas to be cooled; the cooling fan provides cooling air for cooling the cooling pipe.
6. The oil-gas separation system of claim 1, wherein a cyclone is provided at an air inlet of the water separator;
the air inlet of the water separator is sequentially provided with a net pad and a fog pad on a flow path from the air inlet to the air outlet of the water separator, and the fog pad is close to the air outlet of the water separator.
7. The oil and gas separation system of claim 1, further comprising a condensate treatment device;
the gas-liquid separator, the water separator and the low-temperature separator are all provided with liquid discharge ports, and the liquid discharge ports are communicated with the condensate oil treatment device through second pipelines.
8. A method for oil and gas separation, characterized by using the oil and gas separation system of any one of claims 1 to 7, the method comprising the steps of:
s100, feeding the raw material gas into a gas-liquid separator to separate part of heavy hydrocarbon mixture and condensate water from the raw material gas;
s200, feeding the raw material gas separated by the gas-liquid separator into an air cooler for cooling, so that the raw material gas is cooled from a first temperature to a second temperature;
step S300, feeding the raw material gas cooled by the air cooler into a water separator to separate part of light hydrocarbon mixture and condensate water from the raw material gas;
s400, feeding the raw material gas separated by the water separator into a hot gas flow passage of a precooler, and performing heat exchange with dry and cold natural gas separated by a low-temperature separator to reduce the temperature of the raw material gas to a third temperature;
injecting glycol into the hot gas flow channel, and fully mixing the glycol with the raw material gas to reduce the freezing point of the condensed water;
step S500, the raw material gas after heat exchange enters a throttling expansion valve, so that the temperature of the raw material gas is reduced from a third temperature to a fourth temperature, and the pressure is reduced from a first pressure to a second pressure;
step S600; the raw gas after passing through the throttle expansion valve enters a low-temperature separator, and the raw gas is cooled and depressurized in the low-temperature separator, so that part of light hydrocarbon mixture, condensate water and glycol are separated from the raw gas.
9. The oil-gas separation method according to claim 8, wherein before step S100, the moisture of the feed gas is primarily separated.
10. The oil-gas separation method according to claim 8, wherein in the step S400, the flow rate of the dry and cold natural gas flowing into the precooler is adjusted by a temperature control valve, so as to control the temperature and moisture of the raw gas flowing into the throttle expansion valve.
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| CN201910047809.2A CN111456702A (en) | 2019-01-18 | 2019-01-18 | Oil-gas separation system and method |
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Application publication date: 20200728 |