CN211273608U - Low-temperature flash light hydrocarbon recovery system for oilfield associated gas - Google Patents
Low-temperature flash light hydrocarbon recovery system for oilfield associated gas Download PDFInfo
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- CN211273608U CN211273608U CN201921515383.0U CN201921515383U CN211273608U CN 211273608 U CN211273608 U CN 211273608U CN 201921515383 U CN201921515383 U CN 201921515383U CN 211273608 U CN211273608 U CN 211273608U
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Abstract
The utility model relates to a low temperature flash distillation light hydrocarbon recovery system for oil field associated gas, recovery system includes feed gas compressor, adsorption tower, cryogenic heat exchanger, first grade flash separator, second grade flash separator, deethanizer reboiler, liquefied gas tower, reflux drum and liquefied gas tower reboiler; a channel A, a channel B, a channel C and a channel D are arranged in the low-temperature heat exchanger; in this application, the gas that the deethanizer top came out cools off to get into second grade flash separator after the uniform temperature through low temperature heat exchanger once more, the gas of separation satisfies the defeated requirement of dry gas outward, go dry gas low reaches pipe network after low temperature heat exchanger rewarming after mixing with the gas mixture of first-order flash separator separation, liquid that second grade flash separator separation goes the deethanizer after liquid booster pump pressure boost and the liquid mixture of first-order flash separator separation through low temperature heat exchanger rewarming, the rate of recovery of heavy components such as propane, butane, pentane has been improved.
Description
Technical Field
The utility model relates to a processing technology field of oil field associated gas, specifically say, relate to a low temperature flash distillation light hydrocarbon recovery system for oil field associated gas.
Background
The oilfield associated gas is used as an available resource, which means that gas which is generated along with petroleum liquid appears between oil reservoirs in the oilfield during the exploitation process, the main component is methane, and the gas usually contains a large amount of ethane and hydrocarbon heavy components. The recovery treatment of the oilfield associated gas refers to separating out heavy components such as propane, butane and pentane in the gas and selling the heavy components as Liquefied Petroleum Gas (LPG), light oil and other products.
At present, due to the restriction of technical means, associated gas is relatively difficult to control in the process of oil field exploitation, a large part of the associated gas in the oil field is emptied or burnt, the requirements of national safety and environmental protection are not met, and the economic benefit of enterprises is also influenced. The existing associated gas recovery system has the defect of low recovery rate, so that the existing associated gas recovery system needs to be improved and optimized.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the above-mentioned not enough that exists among the prior art, and provide a function perfect, can improve heavy component recovery rates such as propane, butane, can produce the low temperature flash distillation light hydrocarbon recovery system that is used for oil field associated gas of liquefied petroleum gas and light oil product to recovery method has been given.
The utility model provides a technical scheme that above-mentioned problem adopted is: the utility model provides a low temperature flash distillation light hydrocarbon recovery system for oil field associated gas which characterized in that: the device comprises a raw material gas compressor, an adsorption tower I, a low-temperature heat exchanger, a primary flash separator, a secondary flash separator, a deethanizer reboiler, a liquefied gas tower, a reflux tank and a liquefied gas tower reboiler; a channel A, a channel B, a channel C and a channel D are arranged in the low-temperature heat exchanger;
the gas inlet of the raw material gas compressor is communicated with an oilfield associated gas source, the gas outlet of the raw material gas compressor is communicated with the gas inlet of an adsorption tower, the gas outlet of the adsorption tower is communicated with the gas inlet end of a channel C of the low-temperature heat exchanger, the gas outlet end of the channel C is communicated with the gas inlet of a first-stage flash separator, the top gas outlet of the first-stage flash separator is communicated with the gas inlet end of a channel B, the gas outlet end of the channel B is communicated with a dry gas downstream pipe network, the bottom liquid outlet of the first-stage flash separator is communicated with the inlet end of a channel A, and the outlet end of the channel A is communicated,
a top gas outlet of the deethanizer is communicated with a gas inlet end of a channel D, a gas outlet end of the channel D is communicated with a gas inlet of the secondary flash separator, a top gas outlet of the secondary flash separator is communicated with a gas inlet end of a channel B, and a bottom liquid outlet of the secondary flash separator is communicated with an inlet end of a channel A;
a liquid outlet at the bottom of the deethanizer is communicated with a liquid inlet of a reboiler of the deethanizer, a gas outlet of the reboiler of the deethanizer is communicated with a gas inlet of the deethanizer, and a liquid outlet of the reboiler of the deethanizer is communicated with a liquid inlet of a liquefied gas tower;
a top air outlet of the liquefied gas tower is communicated with an air inlet of the reflux tank, and a top air outlet of the reflux tank is communicated with an air inlet of the raw material gas compressor; a liquid outlet at the bottom of the reflux tank is branched into two paths, one path is communicated with a liquid inlet of the liquefied gas tower, and the other path is communicated with a liquefied petroleum gas storage tank;
the liquid outlet at the bottom of the liquefied gas tower is communicated with the liquid inlet of a liquefied gas tower reboiler, the gas outlet of the liquefied gas tower reboiler is communicated with the gas inlet of the liquefied gas tower, and the liquid outlet of the liquefied gas tower reboiler is communicated with a light oil storage tank.
Preferably, the system also comprises a second adsorption tower, the second adsorption tower and the first adsorption tower are arranged side by side, the gas outlet of the feed gas compressor is divided into two paths, one path is communicated with the gas inlet of the first adsorption tower, the other path is communicated with the gas inlet of the second adsorption tower, and valves are arranged on the two paths; and the gas outlet of the second adsorption tower is communicated with the gas inlet end of the channel C of the low-temperature heat exchanger.
Preferably, the air outlet end of the channel B is divided into two paths: the first dry gas path is connected with a dry gas downstream pipe network and is provided with a valve; a regenerated gas heater is arranged on the second dry gas path, the output tail end of the second dry gas path is branched into two paths, the two paths are respectively communicated with the gas outlets of the second adsorption tower and the first adsorption tower, and valves are respectively arranged on the two paths; valves are respectively arranged between the air outlet of the second adsorption tower and the air inlet end of the channel C and between the air outlet of the first adsorption tower and the air inlet end of the channel C; a first regeneration gas path is connected to a connection gas path between the gas outlet of the feed gas compressor and the gas inlet of the first adsorption tower, and a valve is mounted on the first regeneration gas path; a second regeneration gas path is connected to a connection gas path between the gas outlet of the feed gas compressor and the gas inlet of the second adsorption tower, and a valve is mounted on the second regeneration gas path; the output end of the first regeneration gas circuit and the second regeneration gas circuit is connected with the same regeneration gas cooler, the regeneration gas cooler is communicated with a regeneration gas separator, the gas outlet of the regeneration gas separator is communicated with a dry gas downstream pipe network, the liquid outlet of the regeneration gas separator is communicated with an external free water collecting device, and a valve is arranged on the communicating pipe of the liquid outlet of the regeneration gas separator and the external free water collecting device.
Preferably, a liquid booster pump is arranged between a liquid outlet at the bottom of the secondary flash separator and the inlet end of the channel A, and liquid flowing out of the liquid outlet at the bottom of the secondary flash separator enters the channel A for heat exchange after being boosted by the liquid booster pump; the bottom liquid outlet of the first-stage flash separator is communicated with the inlet end of the channel A by first communicating a communicating pipeline between the bottom liquid outlet of the second-stage flash separator and the inlet end of the channel A, and a valve is arranged at the bottom liquid outlet of the first-stage flash separator.
Preferably, a condenser is arranged between the top gas outlet of the liquefied gas tower and the gas inlet of the reflux tank, and gas discharged from the top gas outlet of the liquefied gas tower is condensed by the condenser and cooled and then enters the reflux tank.
Preferably, a delivery pump is installed at a liquid outlet at the bottom of the reflux tank, one path of liquid flowing out of the liquid outlet at the bottom of the reflux tank is delivered to the liquefied gas tower by the delivery pump, and the other path of liquid is delivered to the liquefied petroleum gas storage tank.
Preferably, a liquefied gas cooler is arranged between the liquid outlet of the liquefied gas tower reboiler and the light oil storage tank.
Preferably, the cold energy of the low-temperature heat exchanger is provided by mixed refrigerant, a channel E and a channel F are also arranged in the low-temperature heat exchanger, and the mixed refrigerant enters the channel F after being pressurized and cooled by a refrigerant compressor; the outlet end of the channel F is communicated with the inlet end of the channel E, a low-temperature regulating valve is arranged between the outlet end of the channel F and the inlet end of the channel E, and the outlet end of the channel E is communicated with the inlet end of the refrigerant compressor.
Preferably, the heating heat sources of the deethanizer reboiler and the liquefied gas tower reboiler are respectively provided by heat conducting oil with different temperature positions.
Preferably, the feed gas compressor is a reciprocating compressor, and the refrigerant compressor is a screw compressor; the low-temperature heat exchanger adopts an aluminum plate-fin heat exchanger; the deethanizer and the liquefied gas tower adopt packed towers; and tower bottom reboilers in the deethanizer reboiler and the liquefied gas tower reboiler adopt kettle type heat exchangers.
In order to solve the technical problem, the utility model discloses still provide another technical scheme: a low-temperature flash light hydrocarbon recovery method for oilfield associated gas comprises the following steps:
the first step is as follows: the method comprises the following steps that firstly, oilfield associated gas in an oilfield associated gas source enters a raw gas compressor for pressurization and cooling, and the oilfield associated gas after pressurization and cooling enters a first adsorption tower to remove saturated water in the oilfield associated gas;
the second step is that: the dried oilfield associated gas enters a channel C of a low-temperature heat exchanger for cooling, the cooled oilfield associated gas enters a first-stage flash separator for separation, and heavy components such as propane, butane and pentane in the oilfield associated gas are separated; gas separated from the top of the primary flash separator enters a channel B of the low-temperature heat exchanger for rewarming and then is changed into dry gas to be output, the output dry gas enters a dry gas downstream pipe network, liquid separated from the bottom of the primary flash separator enters a channel A of the low-temperature heat exchanger for cooling and rewarming, and the rewarmed liquid enters a deethanizer for re-separation;
the cold energy of the low-temperature heat exchanger is provided by mixed refrigerant, the mixed refrigerant is composed of four components of methane, ethylene, propane, isobutane and the like, the mixed refrigerant enters a channel F after being pressurized and cooled by a refrigerant compressor, then the mixed refrigerant enters a channel E for providing cold energy for cooling of oilfield associated gas after being throttled and cooled by a low-temperature regulating valve, the mixed refrigerant after being reheated returns to the refrigerant compressor again for pressurization and cooling, and closed cycle compression refrigeration is realized;
the third step: the gas separated from the top of the deethanizer enters a channel D of a low-temperature heat exchanger for cooling, the cooled gas enters a secondary flash separator for re-separation, heavy components such as propane, butane and pentane are separated out, the gas separated from the top of the secondary flash separator and the gas separated from the top of a primary flash separator are mixed and then enter a channel B of the low-temperature heat exchanger for re-heating and then are changed into dry gas for output, the liquid separated from the bottom of the secondary flash separator is pressurized by a liquid booster pump and then is mixed with the liquid separated from the bottom of the primary flash separator, the mixed liquid enters a channel A of the low-temperature heat exchanger for re-heating, and the re-heated liquid enters the deethanizer;
the fourth step: the liquid separated from the bottom of the deethanizer enters a reboiler of the deethanizer, and part of the liquid in the reboiler of the deethanizer is gasified and then returns to the deethanizer as ascending stripping gas; the residual liquid in the reboiler of the deethanizer enters a liquefied gas tower for rectification and separation;
the fifth step: condensing and cooling the gas separated from the top of the liquefied gas tower by a condenser, and then feeding the gas into a reflux tank; after the liquid separated from the reflux tank is pressurized by a delivery pump, one part of the liquid is sent to the top of the liquefied gas tower to be used as reflux liquid in the liquefied gas tower, and the other part of the liquid is sent to a liquefied petroleum gas storage tank for storage; the gas separated from the reflux tank enters a feed gas compressor to realize cyclic recycling;
and a sixth step: the liquid separated from the bottom of the liquefied gas tower enters a liquefied gas tower reboiler, and part of the liquid in the liquefied gas tower reboiler is returned to the liquefied gas tower after being gasified to be used as ascending stripping gas; cooling the residual liquid in the reboiler of the liquefied gas tower by a liquefied gas cooler, and introducing the cooled residual liquid serving as a light oil product into a light oil storage tank for storage;
the seventh step: the first adsorption tower and the second adsorption tower are switched to work circularly in sequence;
when the saturated water adsorbed in the first adsorption tower reaches a certain amount, switching the adsorption towers, allowing the oil field associated gas subjected to pressure boosting and cooling in the first step to enter a second adsorption tower to remove the saturated water in the oil field associated gas, allowing part of dry gas output by a channel B to enter a second dry gas path, opening a valve between the second dry gas path and the first adsorption tower, closing a valve between the second dry gas path and the second adsorption tower, heating the dry gas in the second dry gas path by a regeneration gas heater, allowing the dry gas to enter the first adsorption tower as molecular sieve heating regeneration gas to dry the adsorption towers, allowing the regeneration gas to exit from the first adsorption tower, allowing the regeneration gas to enter a regeneration gas cooler through the first regeneration gas path for cooling, allowing the cooled regeneration gas to enter a regeneration gas separator, mixing the gas separated from the regeneration gas separator with the dry gas in the first dry gas path, and conveying the gas to a dry gas downstream pipe network, the free water separated in the regeneration gas separator is conveyed to an external free water collecting device;
when the saturated water adsorbed in the second adsorption tower reaches a certain amount, the adsorption towers are switched again, the oil field associated gas after being pressurized and cooled in the first step enters the first adsorption tower to remove the saturated water in the oil field associated gas, a valve between the second dry gas path and the first adsorption tower is closed, a valve between the second dry gas path and the second adsorption tower is opened, the dry gas in the second dry gas path is heated by a regeneration gas heater and then enters the second adsorption tower, the regeneration gas is discharged from the second adsorption tower and then enters a regeneration gas cooler through the second regeneration gas path to be cooled, the cooled regeneration gas enters a regeneration gas separator, the gas separated in the regeneration gas separator is mixed with the dry gas in the first dry gas path and then is conveyed to a dry gas downstream pipe network, and the free water separated in the regeneration gas separator is conveyed to an external free water collecting device.
Compared with the prior art, the utility model, have following advantage and effect:
1. the gas from the top of the deethanizer is cooled to a certain temperature again through the low-temperature heat exchanger and then enters the secondary flash separator, the separated gas meets the requirement of dry gas output, the gas is mixed with the gas separated by the primary flash separator and then enters a dry gas downstream pipe network after being reheated through the low-temperature heat exchanger, the liquid separated by the secondary flash separator is pressurized through a liquid booster pump and then is mixed with the liquid separated by the primary flash separator and then enters the deethanizer after being reheated through the low-temperature heat exchanger, and the recovery rate of heavy components such as propane, butane and pentane is improved;
2. the adsorption and dehydration of the oilfield associated gas are carried out by adopting a two-tower switching process, a first adsorption tower and a second adsorption tower are designed, wherein one tower carries out adsorption and dehydration work, the other tower carries out heating regeneration, and a 3A molecular sieve is filled in the towers, so that water is mainly adsorbed, and the adsorption of heavy components is reduced; the working efficiency of the recovery system is improved;
3. the deethanizer and the liquefied gas tower adopt packed towers, and a reboiler at the tower bottom adopts a kettle type heat exchanger, so that the rectification requirements of different gas sources can be met;
4. the low-temperature heat exchanger adopts an aluminum plate-fin heat exchanger, so that the efficiency of the low-temperature heat exchanger is improved;
5. the recovery system and the recovery method can produce LPG and light oil products, reduce the emission of associated gas in an oil field, meet the national requirements on safety and environmental protection, and create economic benefits for enterprises.
Drawings
In order to illustrate the embodiments of the present invention or the solutions in the prior art more clearly, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic structural diagram of a recycling system according to an embodiment of the present invention.
Description of reference numerals:
an oilfield associated gas source 1; a dry gas downstream pipe network 2; a first regeneration gas path 3; a second regeneration gas path 4; an external free water collecting device 5; a liquefied petroleum gas storage tank 6; a light oil storage tank 7; a second dry gas path 8; a first dry gas path 9;
a feed gas compressor 61; a first adsorption column 62; a second adsorption column 63; a cryogenic heat exchanger 64; a primary flash separator 65; a secondary flash separator 66; a liquid booster pump 67; a deethanizer 68; deethanizer reboiler 69; a liquefied gas column 70; a reflux drum 72; a delivery pump 73; a liquefied gas column reboiler 74; a liquefied gas cooler 75; a refrigerant compressor 76; a regeneration gas heater 77; a regeneration gas cooler 78; a regeneration gas separator 79; a low temperature regulating valve 92.
Detailed Description
The present invention will be described in further detail by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not intended to limit the present invention.
Examples are given.
Referring to fig. 1, the embodiment discloses a low-temperature flash light hydrocarbon recovery system for oilfield associated gas, which includes a raw gas compressor 61, a first adsorption tower 62, a second adsorption tower 63, a low-temperature heat exchanger 64, a first-stage flash separator 65, a second-stage flash separator 66, a deethanizer 68, a deethanizer reboiler 69, a liquefied gas tower 70, a reflux tank 72, and a liquefied gas tower reboiler 74.
In this embodiment, the low-temperature heat exchanger 64 is an aluminum plate-fin heat exchanger, and a channel a, a channel B, a channel C, a channel D, a channel E, and a channel F are provided therein. The cold energy of the low-temperature heat exchanger 64 is provided by mixed refrigerant, the mixed refrigerant is composed of four components of methane, ethylene, propane, isobutane and the like, the refrigerant compressor 76 adopts a screw compressor, and the mixed refrigerant enters the channel F after being pressurized and cooled by the refrigerant compressor 76; the outlet end of the passage F is communicated with the inlet end of the passage E, and a low-temperature regulating valve 92 is installed between the outlet end of the passage F and the inlet end of the passage E, the low-temperature regulating valve 92 is used for regulating the pressure and the flow of the mixed refrigerant to achieve the purpose of throttling, and the outlet end of the passage E is communicated with the inlet end of the refrigerant compressor 76.
In this embodiment, the mixed refrigerant is supercharged and cooled by the refrigerant compressor 76 and then enters the passage F, and then is throttled and cooled by the low-temperature regulating valve 92, the low-pressure mixed refrigerant enters the passage E to provide cooling capacity for cooling of oilfield associated gas, and the reheated mixed refrigerant returns to the refrigerant compressor 76 again for supercharging and cooling, so that closed cycle compression refrigeration is realized.
In this embodiment, the first adsorption tower 62 and the second adsorption tower 63 are arranged side by side, the raw material gas compressor 61 adopts a reciprocating compressor, the gas inlet of the raw material gas compressor 61 is connected with the oilfield associated gas source 1, the gas outlet of the raw material gas compressor 61 is divided into two paths, one path is connected with the gas inlet of the first adsorption tower 62, the other path is connected with the gas inlet of the second adsorption tower 63, and a valve is installed on the two paths. The oilfield associated gas is pressurized and cooled by a raw material gas compressor 61 and then needs to enter an adsorption tower to remove saturated water.
In this embodiment, the first adsorption tower 62 and the second adsorption tower 63 are sequentially switched to operate, one tower performs adsorption and dehydration, the other tower performs heating and regeneration, the gas outlet of the first adsorption tower 62 and the gas outlet of the second adsorption tower 63 are both connected to the gas inlet end of the channel C of the low temperature heat exchanger 64, when the two towers operate, only one of the towers can be connected to the channel C of the low temperature heat exchanger 64, and the two towers cannot simultaneously introduce oilfield associated gas into the channel C.
In this embodiment, the gas outlet of the channel C is connected to the gas inlet of the first-stage flash separator 65, the gas outlet at the top of the first-stage flash separator 65 is connected to the gas inlet of the channel B, the liquid outlet at the bottom of the first-stage flash separator 65 is connected to the inlet of the channel a, and the outlet of the channel a is connected to the liquid inlet of the deethanizer 68.
In this embodiment, the air outlet end of the channel B is divided into two paths: the first dry gas path 9 is communicated with the dry gas downstream pipe network 2, and the second dry gas path 8 is provided with a valve; the second dry gas path 8 is provided with a regeneration gas heater 77, and the output end of the second dry gas path 8 is branched into two paths, the two paths are respectively communicated with the gas outlets of the second adsorption tower 63 and the first adsorption tower 62, and the two paths are respectively provided with a valve. Valves are arranged between the air outlet of the second adsorption tower 63 and the air inlet end of the channel C, and between the air outlet of the first adsorption tower 62 and the air inlet end of the channel C.
In this embodiment, a first regeneration gas path 3 is connected to a connection gas path between the gas outlet of the raw gas compressor 61 and the gas inlet of the first adsorption tower 62, and a valve is installed on the first regeneration gas path 3. A second regeneration gas path 4 is connected to a connection gas path between the gas outlet of the raw gas compressor 61 and the gas inlet of the second adsorption tower 63, and a valve is installed on the second regeneration gas path 4. The output tail ends of the first regeneration gas circuit 3 and the second regeneration gas circuit 4 are connected with the same regeneration gas cooler 78, the regeneration gas cooler 78 is communicated with a regeneration gas separator 79, the gas outlet of the regeneration gas separator 79 is communicated with a dry gas downstream pipe network 2, the liquid outlet of the regeneration gas separator 79 is communicated with an external free water collecting device 5, and a valve is arranged on a communicating pipe between the liquid outlet of the regeneration gas separator 79 and the external free water collecting device 5.
In this embodiment, the top gas outlet of the deethanizer 68 is connected to the gas inlet of the channel D, the gas outlet of the channel D is connected to the gas inlet of the secondary flash separator 66, the top gas outlet of the secondary flash separator 66 is connected to the gas inlet of the channel B, and the bottom liquid outlet of the secondary flash separator 66 is connected to the inlet of the channel a.
In this embodiment, a liquid outlet at the bottom of the deethanizer 68 is connected to a liquid inlet of a deethanizer reboiler 69, a gas outlet of the deethanizer reboiler 69 is connected to a gas inlet of the deethanizer 68, and a liquid outlet of the deethanizer reboiler 69 is connected to a liquid inlet of the liquefied gas tower 70.
In this embodiment, a liquid booster pump 67 is installed between the bottom liquid outlet of the secondary flash separator 66 and the inlet end of the passage a, and the liquid flowing out of the bottom liquid outlet of the secondary flash separator 66 enters the passage a for heat exchange after being boosted by the liquid booster pump 67. The bottom liquid outlet of the first-stage flash separator 65 is communicated with the inlet end of the channel a by first communicating a communicating pipeline between the bottom liquid outlet of the second-stage flash separator 66 and the inlet end of the channel a, and a valve is arranged at the bottom liquid outlet of the first-stage flash separator 65.
In this embodiment, the top air outlet of the liquefied gas tower 70 is connected to the air inlet of the reflux tank 72, a condenser 71 is installed between the top air outlet and the reflux tank 72, and the gas discharged from the top air outlet of the liquefied gas tower 70 is condensed by the condenser 71 to be cooled and then enters the reflux tank 72. The top outlet of the reflux tank 72 is communicated with the inlet of the raw material gas compressor 61.
In this embodiment, the liquid outlet at the bottom of the reflux tank 72 is branched into two paths, one path is connected to the liquid inlet of the liquefied gas tower 70, and the other path is connected to the liquefied petroleum gas storage tank 6. A delivery pump 73 is arranged at a liquid outlet at the bottom of the reflux tank 72, one path of liquid flowing out of the liquid outlet at the bottom of the reflux tank 72 is delivered to the liquefied gas tower 70 by the delivery pump 73, and the other path of liquid is delivered to the liquefied petroleum gas storage tank 6.
In this embodiment, a liquid outlet at the bottom of the liquefied gas tower 70 is connected with a liquid inlet of the liquefied gas tower reboiler 74, a gas outlet of the liquefied gas tower reboiler 74 is connected with a gas inlet of the liquefied gas tower 70, and a liquid outlet of the liquefied gas tower reboiler 74 is connected with the light oil storage tank 7. A liquefied gas cooler 75 is installed between the liquid outlet of the liquefied gas tower reboiler 74 and the light oil storage tank 7.
In this embodiment, the heating heat sources of the deethanizer reboiler 69 and the liquefied gas tower reboiler 74 are respectively provided by heat transfer oils of different temperature levels; the deethanizer 68 and the liquefied gas column 70 employ packed columns; the reboiler at the bottom of the deethanizer reboiler 69 and the liquefied gas column reboiler 74 employs a tank heat exchanger.
The embodiment also discloses a low-temperature flash light hydrocarbon recovery method for the oilfield associated gas, which comprises the following steps:
the first step is as follows: the method comprises the following steps that (1) oilfield associated gas in an oilfield associated gas source 1 firstly enters a raw gas compressor 61 for pressurization and cooling, and the oilfield associated gas after pressurization and cooling enters a first adsorption tower 62 for removing saturated water in the oilfield associated gas;
the second step is that: the dried oilfield associated gas enters a channel C of the low-temperature heat exchanger 64 for cooling, the cooled oilfield associated gas enters a first-stage flash separator 65 for separation, and heavy components such as propane, butane and pentane in the oilfield associated gas are separated; the gas separated from the top of the primary flash separator 65 enters a channel B of the low-temperature heat exchanger 64 for rewarming and then is changed into dry gas to be output, the output dry gas enters a dry gas downstream pipe network 2, the liquid separated from the bottom of the primary flash separator 65 enters a channel A of the low-temperature heat exchanger 64 for cooling and rewarming, and the rewarmed liquid enters a deethanizer 68 for re-separation;
the cold energy of the low-temperature heat exchanger 64 is provided by mixed refrigerant, the mixed refrigerant is composed of four components of methane, ethylene, propane, isobutane and the like, the mixed refrigerant enters the channel F after being pressurized and cooled by the refrigerant compressor 76, then the mixed refrigerant enters the channel E for providing cold energy for cooling of oilfield associated gas after being throttled and cooled by the low-temperature regulating valve 92, the mixed refrigerant after being reheated returns to the refrigerant compressor 76 for pressurization and cooling again, and closed cycle compression refrigeration is realized;
the third step: the gas separated from the top of the deethanizer 68 enters a channel D of the low-temperature heat exchanger 64 for cooling, the cooled gas enters a secondary flash separator 66 for re-separation, heavy components such as propane, butane and pentane are separated out, the gas separated from the top of the secondary flash separator 66 is mixed with the gas separated from the top of the primary flash separator 65, the mixture enters a channel B of the low-temperature heat exchanger 64 for re-heating and is changed into dry gas for output, the liquid separated from the bottom of the secondary flash separator 66 is pressurized by a liquid booster pump 67 and then is mixed with the liquid separated from the bottom of the primary flash separator 65, the mixed liquid enters a channel A of the low-temperature heat exchanger 64 for re-heating, and the re-heated liquid enters the deethanizer 68;
the fourth step: the liquid separated from the bottom of the deethanizer 68 enters a deethanizer reboiler 69, and part of the liquid in the deethanizer reboiler 69 is gasified and then returns to the deethanizer 68 to be used as ascending stripping gas; the residual liquid in the deethanizer reboiler 69 enters a liquefied gas tower 70 for rectification and separation;
the fifth step: the gas separated from the top of the liquefied gas tower 70 is condensed and cooled by a condenser 71 and then enters a reflux tank 72; after the liquid separated from the reflux tank 72 is pressurized by a delivery pump 73, a part of the liquid is sent to the top of the liquefied gas tower 70 to be used as reflux liquid in the liquefied gas tower, and the other part of the liquid is sent to the liquefied petroleum gas storage tank 6 for storage; the gas separated from the reflux tank 72 enters the raw material gas compressor 61 to realize recycling;
and a sixth step: the liquid separated from the bottom of the liquefied gas tower 70 enters a liquefied gas tower reboiler 74, and after part of the liquid in the liquefied gas tower reboiler 74 is gasified, the liquid returns to the liquefied gas tower 70 to be used as ascending stripping gas; the liquid remaining in the liquefied gas tower reboiler 74 is cooled by a liquefied gas cooler 75 and then introduced into the light oil storage tank 7 as a light oil product for storage;
the seventh step: the first adsorption tower 62 and the second adsorption tower 63 are switched to work circularly in sequence;
when the saturated water adsorbed in the first adsorption tower 62 reaches a certain amount, switching the adsorption towers, allowing the oil field associated gas subjected to pressure boosting and cooling in the first step to enter a second adsorption tower 63 to remove the saturated water in the oil field associated gas, allowing a part of dry gas output from a channel B to enter a second dry gas path 8, opening a valve between the second dry gas path 8 and the first adsorption tower 62, closing a valve between the second dry gas path 8 and the second adsorption tower 63, allowing the dry gas in the second dry gas path 8 to enter the first adsorption tower 62 as molecular sieve heating and regenerating gas to dry the adsorption towers after being heated by a regenerating gas heater 77, allowing the regenerating gas to exit the first adsorption tower 62, allowing the regenerating gas to enter a regenerating gas cooler 78 through a regenerating gas path 3 for cooling, allowing the cooled regenerating gas to enter a regenerating gas separator 79, mixing the gas separated from the regenerating gas separator 79 with the dry gas in the first dry gas path 9, and conveying the gas to a dry gas downstream pipe network 2, the free water separated in the regeneration gas separator 79 is sent to the external free water collecting device 5;
when the saturated water adsorbed in the second adsorption tower 63 reaches a certain amount, the adsorption towers are switched again, the oil field associated gas after being pressurized and cooled in the first step enters the first adsorption tower 62 to remove the saturated water in the oil field associated gas, a valve between the second dry gas path 8 and the first adsorption tower 62 is closed, a valve between the second dry gas path 8 and the second adsorption tower 63 is opened, the dry gas in the second dry gas path 8 enters the second adsorption tower 63 after being heated by a regenerated gas heater 77, the regenerated gas exits from the second adsorption tower 63 and enters a regenerated gas cooler 78 through a second regenerated gas path 4 to be cooled, the cooled regenerated gas enters a regenerated gas separator 79, the gas separated in the regeneration gas separator 79 is mixed with the dry gas in the first dry gas path 9 and then conveyed to the dry gas downstream pipe network 2, and the free water separated in the regeneration gas separator 79 is conveyed to the external free water collecting device 5.
In addition, it should be noted that the specific embodiments described in the present specification may be different in the components, the shapes of the components, the names of the components, and the like, and the above description is only an example of the structure of the present invention. All the equivalent changes or simple changes made according to the structure, characteristics and principle of the utility model are included in the protection scope of the utility model. Various modifications, additions and substitutions may be made by those skilled in the art without departing from the scope of the invention as defined in the accompanying claims.
Claims (10)
1. The utility model provides a low temperature flash distillation light hydrocarbon recovery system for oil field associated gas which characterized in that: comprises a raw material gas compressor (61), a first adsorption tower (62), a low-temperature heat exchanger (64), a first-stage flash separator (65), a second-stage flash separator (66), a deethanizer (68), a deethanizer reboiler (69), a liquefied gas tower (70), a reflux tank (72) and a liquefied gas tower reboiler (74);
a channel A, a channel B, a channel C and a channel D are arranged in the low-temperature heat exchanger (64);
the gas inlet of the raw gas compressor (61) is communicated with an oilfield associated gas source (1), the gas outlet of the raw gas compressor (61) is communicated with the gas inlet of an adsorption tower (62), the gas outlet of the adsorption tower (62) is communicated with the gas inlet end of a channel C of a low-temperature heat exchanger (64), the gas outlet end of the channel C is communicated with the gas inlet of a first-stage flash separator (65), the top gas outlet of the first-stage flash separator (65) is communicated with the gas inlet end of a channel B, the gas outlet end of the channel B is communicated with a dry gas downstream pipe network (2), the bottom liquid outlet of the first-stage flash separator (65) is communicated with the inlet end of the channel A, and the outlet end of the channel A is communicated with the liquid inlet of a dee,
a top gas outlet of the deethanizer (68) is communicated with a gas inlet end of a channel D, a gas outlet end of the channel D is communicated with a gas inlet of the secondary flash separator (66), a top gas outlet of the secondary flash separator (66) is communicated with a gas inlet end of a channel B, and a bottom liquid outlet of the secondary flash separator (66) is communicated with an inlet end of a channel A;
a liquid outlet at the bottom of the deethanizer (68) is communicated with a liquid inlet of a deethanizer reboiler (69), a gas outlet of the deethanizer reboiler (69) is communicated with a gas inlet of the deethanizer (68), and a liquid outlet of the deethanizer reboiler (69) is communicated with a liquid inlet of a liquefied gas tower (70);
a top air outlet of the liquefied gas tower (70) is communicated with an air inlet of the reflux tank (72), and a top air outlet of the reflux tank (72) is communicated with an air inlet of the raw material gas compressor (61); a liquid outlet at the bottom of the reflux tank (72) is branched into two paths, one path is communicated with a liquid inlet of the liquefied gas tower (70), and the other path is communicated with a liquefied petroleum gas storage tank (6);
the liquid outlet at the bottom of the liquefied gas tower (70) is communicated with the liquid inlet of a liquefied gas tower reboiler (74), the gas outlet of the liquefied gas tower reboiler (74) is communicated with the gas inlet of the liquefied gas tower (70), and the liquid outlet of the liquefied gas tower reboiler (74) is communicated with the light oil storage tank (7).
2. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: the system also comprises a second adsorption tower (63), wherein the second adsorption tower (63) and the first adsorption tower (62) are arranged side by side, the gas outlet of the raw material gas compressor (61) is divided into two paths, one path is communicated with the gas inlet of the first adsorption tower (62), the other path is communicated with the gas inlet of the second adsorption tower (63), and valves are arranged on the two paths; the gas outlet of the second adsorption tower (63) is communicated with the gas inlet end of the channel C of the low-temperature heat exchanger (64).
3. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 2, wherein: the air outlet end of the channel B is divided into two paths: the first dry gas path (9) and the second dry gas path (8), wherein the first dry gas path (9) is communicated with a dry gas downstream pipe network (2), and a valve is arranged on the gas paths;
a regenerated gas heater (77) is installed on the second dry gas path (8), the output tail end of the second dry gas path (8) is branched into two paths, the two paths are respectively communicated with the gas outlets of the second adsorption tower (63) and the first adsorption tower (62), and valves are respectively installed on the two paths;
valves are respectively arranged between the air outlet of the second adsorption tower (63) and the air inlet end of the channel C, and between the air outlet of the first adsorption tower (62) and the air inlet end of the channel C;
a first regeneration gas path (3) is connected to a connection gas path between the gas outlet of the raw material gas compressor (61) and the gas inlet of the first adsorption tower (62), and a valve is mounted on the first regeneration gas path (3);
a second regeneration gas path (4) is connected to a connection gas path between the gas outlet of the feed gas compressor (61) and the gas inlet of the second adsorption tower (63), and a valve is mounted on the second regeneration gas path (4);
the output end of a regeneration gas circuit (3) and No. two regeneration gas circuits (4) is connected with the same regeneration gas cooler (78), the regeneration gas cooler (78) is communicated with a regeneration gas separator (79), the gas outlet of the regeneration gas separator (79) is communicated with a dry gas downstream pipeline network (2), the liquid outlet of the regeneration gas separator (79) is communicated with an external free water collecting device (5), and a valve is arranged on a communicating pipeline of the liquid outlet of the regeneration gas separator (79) and the external free water collecting device (5).
4. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: a liquid booster pump (67) is arranged between a liquid outlet at the bottom of the secondary flash separator (66) and an inlet end of the channel A, and liquid flowing out of a liquid outlet at the bottom of the secondary flash separator (66) enters the channel A for heat exchange after being boosted by the liquid booster pump (67);
the bottom liquid outlet of the first-stage flash separator (65) is communicated with the inlet end of the channel A by first communicating a communicating pipeline between the bottom liquid outlet of the second-stage flash separator (66) and the inlet end of the channel A, and a valve is arranged at the bottom liquid outlet of the first-stage flash separator (65).
5. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: a condenser (71) is arranged between a top air outlet of the liquefied gas tower (70) and an air inlet of the reflux tank (72), and gas discharged from the top air outlet of the liquefied gas tower (70) is condensed by the condenser (71) to be cooled and then enters the reflux tank (72).
6. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: and a liquid outlet at the bottom of the reflux tank (72) is provided with a conveying pump (73), one path of liquid flowing out of the liquid outlet at the bottom of the reflux tank (72) is conveyed to the liquefied gas tower (70) by the conveying pump (73), and the other path of liquid is conveyed to the liquefied petroleum gas storage tank (6).
7. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: and a liquefied gas cooler (75) is arranged between the liquid outlet of the liquefied gas tower reboiler (74) and the light oil storage tank (7).
8. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 1, wherein: the cold energy of the low-temperature heat exchanger (64) is provided by mixed refrigerant, a channel E and a channel F are also arranged in the low-temperature heat exchanger (64), and the mixed refrigerant enters the channel F after being pressurized and cooled by a refrigerant compressor (76); the outlet end of the channel F is communicated with the inlet end of the channel E, a low-temperature regulating valve (92) is arranged between the outlet end of the channel F and the inlet end of the channel E, and the outlet end of the channel E is communicated with the inlet end of a refrigerant compressor (76).
9. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 8, wherein: and heating heat sources of the deethanizer reboiler (69) and the liquefied gas tower reboiler (74) are respectively provided by heat conduction oil with different temperature positions.
10. The low-temperature flash light hydrocarbon recovery system for oilfield associated gas of claim 8, wherein: the feed gas compressor (61) adopts a reciprocating compressor, and the refrigerant compressor (76) adopts a screw compressor; the low-temperature heat exchanger (64) adopts an aluminum plate-fin heat exchanger; the deethanizer (68) and the liquefied gas tower (70) adopt packed towers; and the reboiler at the bottom of the deethanizer reboiler (69) and the reboiler at the bottom of the liquefied gas tower (74) adopts a kettle type heat exchanger.
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| CN110538476A (en) * | 2019-09-11 | 2019-12-06 | 杭州宏盛中弘新能源有限公司 | Low-temperature flash light hydrocarbon recovery system and method for oilfield associated gas |
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