CN116481261A - Method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon - Google Patents

Method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon Download PDF

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Publication number
CN116481261A
CN116481261A CN202310498337.9A CN202310498337A CN116481261A CN 116481261 A CN116481261 A CN 116481261A CN 202310498337 A CN202310498337 A CN 202310498337A CN 116481261 A CN116481261 A CN 116481261A
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China
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natural gas
benzene
light hydrocarbon
raw material
propane
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李春秀
刘元直
周政
许桂琴
孟令华
许艳赫
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China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
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    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
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    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0645—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
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Abstract

The invention relates to a method for recovering benzene-containing natural gas medium-pressure deep-cooling light hydrocarbons, and belongs to the technical field of natural gas treatment. The invention discloses a method for recycling benzene-containing natural gas medium-pressure cryogenic light hydrocarbons, which comprises the following steps: pressurizing raw material natural gas, drying, dehydrating, performing cryogenic separation, throttling and expanding a liquid phase part obtained by the cryogenic separation through a J-T valve, and then sending the liquid phase part into a demethanizer to separate methane; the liquid phase obtained by low-temperature separation before the J-T valve or the raw material natural gas before the low-temperature separation is mixed with C3-C5 alkane. According to the benzene-containing natural gas medium-pressure cryogenic light hydrocarbon recovery method, liquid phase obtained by low-temperature separation before the J-T valve or raw material natural gas upstream of the low-temperature separator is mixed with C3-C5 alkane, so that the temperature of separating out benzene from materials can be reduced by intervention without introducing other substances, and the problem that the J-T valve of the natural gas medium-pressure cryogenic light hydrocarbon recovery device is frozen and blocked due to the fact that the raw material natural gas contains benzene is solved.

Description

Method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon
Technical Field
The invention relates to a method for recovering benzene-containing natural gas medium-pressure deep-cooling light hydrocarbons, and belongs to the technical field of natural gas treatment.
Background
The natural gas medium-pressure deep-cooling light hydrocarbon recovery device adopts a mixed refrigeration process of propane and an expander, raw material gas is compressed to 4.5MPa by a compression unit and dehydrated, then enters an NGL recovery unit, is subjected to propane refrigerant refrigeration and expander expansion refrigeration to-80 ℃ in sequence, and the cooled raw material gas enters a rectifying tower to carry out light hydrocarbon recovery operation. Along with the development of crude oil to heavy oil increasing direction in the middle and later stages of crude oil extraction, the associated gas quantity gradually decreases, and light hydrocarbon substances in the associated gas gradually decrease. The change of the gas quantity and the gas quality increases the operation difficulty of the natural gas treatment device, enhances the throttling and cooling effects of the J-T valve, reduces the temperature after the valve and is easy to cause the freezing and blocking phenomenon. When the freezing and blocking phenomenon is serious, the raw gas compressor and the expansion booster are stopped, the device is difficult to safely and stably run, and even the whole plant is stopped. If the general defrosting agent is introduced, the defrosting agent is injected to a position where a frost plug is formed by injecting the defrosting agent, so that the aim of defrosting is achieved. Then other components besides natural gas are introduced into the system, subsequent equipment is required to be added for removal, the process is complex, the operation difficulty is increased, and the construction investment and the operation cost are increased.
Disclosure of Invention
The invention aims to provide a method for recycling benzene-containing natural gas medium-pressure deep-cooling light hydrocarbons, which can solve the problem of freezing blockage after a J-T valve of a device caused by poor quality of raw material natural gas without introducing impurities.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
a method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon comprises the following steps: pressurizing raw material natural gas, drying, dehydrating, cryogenic cooling, sending into a low-temperature separator for low-temperature separation, and sending a liquid phase obtained by the low-temperature separation into a dealkylation tower after throttling expansion through a J-T valve; mixing C3-C5 alkane into liquid phase obtained by low-temperature separation before a J-T valve or raw natural gas upstream of a low-temperature separator; the alkane is one or more of propane, butane and pentane.
According to the benzene-containing natural gas medium-pressure cryogenic light hydrocarbon recovery method, liquid phase obtained by low-temperature separation before the J-T valve or raw material natural gas upstream of the low-temperature separator is mixed with C3-C5 alkane, so that the temperature (the freezing and blocking temperature of benzene) for reducing the separation of benzene from materials can be achieved while other substances are not introduced, and the problem that the freezing and blocking occur after the J-T valve of the natural gas medium-pressure cryogenic light hydrocarbon recovery device is caused by the poor quality of the raw material natural gas is relieved/solved.
In order to thoroughly solve the problem of freezing and blocking after the J-T valve of the device caused by the poor quality of the raw material natural gas, further, the mixing amount of alkane can lead the precipitation temperature of benzene in the material flowing through the J-T valve to be lower than the temperature of the material after throttling expansion through the J-T valve. For example, the alkane is incorporated in an amount of not more than 40% by mass, for example, 17 to 20% by mass, of the raw natural gas. Further, an alkane is mixed into the raw natural gas before pressurization. The alkane is mixed in the raw material natural gas before pressurization, so that the effective control on the freezing and blocking of the device can be realized under the conditions of ensuring less modification to the original process and less increase in investment, the running reliability of the device is improved, the yield of subsequent ethane products is improved, and the system is not disturbed.
It is understood that the C3-C5 alkane is one or any of propane, butane and pentane. Further, the propane, butane and pentane are all products of the benzene-containing natural gas medium pressure cryogenic light hydrocarbon recovery method.
Further, a C3-C5 alkane is mixed into the raw natural gas before pressurization. The raw material gas is input into a raw material gas buffer tank for buffering and then is pressurized, and the C3-C5 alkane is input into the raw material buffer tank for mixing the C3-C5 alkane into the raw material natural gas. The disturbance of the mixture of the C3-C5 alkane to the system can be reduced by conveying the C3-C5 alkane into the raw material buffer tank, the stability of the system is improved, and especially when the conventional natural gas medium-pressure cryogenic light hydrocarbon recovery device is modified to implement the recovery method of the invention, the disturbance of the mixture of the C3-C5 alkane to the system can be obviously reduced, the stability of the system is improved, the modification investment is reduced, and the production cost is reduced.
The C3-C5 alkane of the benzene-containing natural gas medium-pressure cryogenic light hydrocarbon recovery product is mixed into the raw material natural gas before pressurization, so that gasification can occur. As the temperature after the J-T valve is about-101 ℃, the light hydrocarbon product is about normal temperature, and the basic parameters of the J-T valve and the light hydrocarbon product are very different, equipment such as a condenser, a compressor and the like are required to be added in the middle when the thawing agent is mixed from other positions in order to ensure that the operation parameters of the device are unchanged, and the equipment investment is increased.
The dealkanizer can be set according to specific production requirements, and can be used for demethanizing or demethanizing and ethane. Further, the dealkylation tower is a demethanizer, and the method for recovering the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon further comprises the following steps: and sending the extracting solution of the tower kettle of the demethanizer into the deethanizer for separating ethane, and sending the extracting solution of the tower kettle of the deethanizer into the depropanizer for separating propane. Further, mixing part of propane separated by the depropanizer into raw natural gas before pressurization; and/or storing the propane separated from the depropanizer in a propane tank, and transporting the propane in the propane tank to mix into the raw natural gas prior to pressurization.
Further, the method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon further comprises the following steps: and (3) sending the extract of the bottom of the depropanizer into the debutanizer for separating butane. Further, mixing a portion of the butane separated from the debutanizer into the raw natural gas prior to pressurization; and/or storing butane separated from the debutanizer in a butane storage tank, and transporting butane in the butane storage tank to be mixed into the raw natural gas before pressurization.
Further, the method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon further comprises the following steps: and feeding the extract of the bottom of the debutanizer into a depentanizer for separating pentane. Further, mixing part of pentane separated by the depentanizer into the raw natural gas before pressurization; and/or storing the pentane separated from the depentanizer in a pentane storage tank, and transporting the pentane in the pentane storage tank into the raw natural gas before pressurization.
Drawings
FIG. 1 is a schematic diagram of a recovery device used in a conventional natural gas medium pressure cryogenic light hydrocarbon recovery method;
FIG. 2 is a schematic diagram of a recovery device used in the method for recovering light hydrocarbons by using middle-pressure cryogenic natural gas containing benzene in example 1 of the present invention;
FIG. 3 is a schematic diagram of a recovery device used in the method for recovering light hydrocarbons by using middle-pressure cryogenic natural gas containing benzene in example 2 of the present invention;
FIG. 4 is a schematic diagram of a recovery device used in the method for recovering light hydrocarbons by using middle-pressure cryogenic natural gas containing benzene in example 3 of the present invention;
wherein, the V01-raw material gas buffer tank, the V02-primary compression buffer tank, the V03-secondary compression buffer tank, the V04-low temperature separator, the V05-ethane condensate buffer tank, the V06-propane condensate buffer tank, the V07-butane condensate buffer tank, the V08-pentane condensate buffer tank, the V09A/V09B-drying tower, the E01-cold box, the E02-primary compression air cooler, the E03-secondary compression air cooler, a reboiler matched with the E04-demethanizer, the E05-ethane condenser, the E06-propane condenser, the E07-butane condenser, the E08-pentane condenser and a reboiler matched with the E09-deethanizer, the system comprises a reboiler matched with an E10-depropanizer, a reboiler matched with an E11-debutanizer, a reboiler matched with an E12-depentanizer, an E13-secondary compression heat exchanger, a K1-primary compressor, a 2TK 1-secondary compressor, a 2TK 2-expander, a P01-booster pump, a P02-ethane reflux pump, a P03-propane reflux pump, a P04-butane reflux pump, a P05-pentane reflux pump, a F01-filter, a T101-demethanizer, a T102-deethanizer, a T103-depropanizer, a T104-debutanizer, a T105-depentanizer, a V21/V22-propane storage tank, a V31/V32-butane storage tank and a V41/V42-pentane storage tank.
Detailed Description
The technical scheme of the invention is further described below with reference to the specific embodiments.
The recovery device adopted by the existing natural gas medium-pressure cryogenic light hydrocarbon recovery method is shown in fig. 1, and comprises a raw gas buffer unit, a raw gas compression unit, a drying unit, a recovery unit and a storage unit, wherein the raw gas buffer unit, the raw gas compression unit, the drying unit and the recovery unit are sequentially arranged in the material flow direction; the raw material gas buffer unit comprises a raw material gas buffer tank V01, the raw material gas compression unit comprises a first-stage compressor K1, a first-stage compression air cooler E02, a first-stage compression buffer tank V02, a second-stage compressor 2TK1, a second-stage compression air cooler E03, a second-stage compression heat exchanger E13 and a second-stage compression buffer tank V03 which are sequentially arranged in the material flow direction, and a raw material gas outlet of the raw material gas buffer tank V01 is connected with an air inlet of the first-stage compressor K1; the drying unit comprises drying towers V09A and V09B which are connected in parallel, and the raw material inlets of the drying towers V09A and V09B are connected with the raw material gas outlet of the secondary compression buffer tank V03;
the recovery unit comprises a cold box E01, a low-temperature separator V04, a demethanizer T101, a deethanizer T102, a depropanizer T103, a debutanizer T104 and a depentanizer T105; the raw material gas inlet of the cold box E01 is connected with the raw material gas outlets of the drying towers V09A and V09B through pipelines, a filter F01 is arranged on the connecting pipeline, a branch pipeline is arranged on the connecting pipeline at the downstream of the filter F01, the branch pipeline is connected with the heating fluid inlet of a reboiler E04 matched with the demethanizer, and the heating fluid outlet of the reboiler E04 matched with the demethanizer is connected with a raw material natural gas channel in the cold box; the feed gas outlet of the cold box E01 is connected with the feed inlet of the low-temperature separator V04 through a pipeline, the liquid phase outlet and the gas phase outlet of the low-temperature separator V04 are both connected with the demethanizer T101, in order to cool the liquid phase and the gas phase separated by the low-temperature separator V04 by using the cold box E01, the cold box E01 is respectively provided with a liquid phase flow channel and a gas phase flow channel for cooling the liquid phase and the gas phase separated by the low-temperature separator V04, the liquid phase outlet of the low-temperature separator V04 is connected with the inlet of the liquid phase flow channel through a pipeline, and the gas phase outlet is connected with the inlet of the gas phase flow channel through a pipeline; the outlet of the liquid phase flow channel is connected with a liquid phase feed inlet at the top of the demethanizer T101 through a pipeline, and a J-T valve is arranged on the connecting pipeline; the outlet of the gas phase flow channel is also connected with the other feeding port on the top of the T101 through a pipeline, and an expander 2TK2 is arranged on the connecting pipeline; the cold box 01 is also provided with a T101 tower kettle extract flow channel for heating the T101 tower kettle extract, the inlet of the flow channel is connected with the extraction port of the tower kettle of T101 through a pipeline, the connecting pipeline is provided with a booster pump P01, and the outlet of the connecting channel is connected with the feed inlet of the deethanizer T102 through a pipeline; the method comprises the steps that an ethane condenser E05, an ethane condensate buffer tank V05 and an ethane reflux pump P02 which are sequentially arranged are arranged on the top of a deethanizer T102 in a matched mode, a reboiler E09 which is sequentially arranged on the bottom of the deethanizer T102 is arranged, a pumping pipeline of the bottom of the deethanizer T102 is connected with a feed inlet of a depropanizer T103, a propane condenser E06, a propane condensate buffer tank V06 and a propane reflux pump P03 which are sequentially arranged on the top of the depropanizer T103 in a matched mode are arranged on the top of the depropanizer T103 in a matched mode, a reboiler E10 which is sequentially arranged on the bottom of the depropanizer T103 is arranged on the bottom of the deethanizer T104, a butane condenser E07, a butane condensate buffer tank V07 and a butane reflux pump P04 which are sequentially arranged on the bottom of the deethanizer T104 are sequentially arranged, a pumping pipeline of the bottom of the depropanizer T104 is connected with a feed inlet of a depropanizer T105, a pentane condenser E08 and a pentane condensate buffer tank E08 are sequentially arranged on the bottom of the depropanizer T105; the storage unit comprises propane storage tanks V21 and V22, butane storage tanks V31 and V32 and pentane storage tanks V41 and V42, wherein a feed inlet of the propane storage tank is connected with a top reflux pipeline of the depropanizer T103, a feed inlet of the butane storage tank is connected with a top reflux pipeline of the debutanizer T104, a feed inlet of the pentane storage tank is connected with a top reflux pipeline of the depentanizer T105, and ethane products produced by the deethanizer are directly output.
When the recovery device is used for recovering the middle-pressure deep-cooling light hydrocarbon of the benzene-containing natural gas, the J-T valve is easy to be frozen and blocked. The inventor carries out analysis and calculation on the freezing and plugging points of light hydrocarbon components which are easy to precipitate solids in the materials behind the J-T valve, finds that the freezing and plugging temperature of benzene is highest, proves that benzene is the component which is easy to precipitate solids, and the freezing and plugging points of benzene are consistent with the freezing and plugging temperature of the pipeline behind the J-T valve recorded on site, and further determines that the component which causes the pipeline to be frozen and plugged behind the J-T valve is benzene. This is because, as the associated gas becomes depleted in quality, in the compression unit of the natural gas medium pressure cryogenic light hydrocarbon recovery device, the dissolution capacity of benzene in the system tends to be weakened due to the vapor-liquid phase equilibrium, and a part of benzene enters the gas phase, so that the gas phase partial pressure of benzene increases. And as the gas phase enters the subsequent recovery unit, the temperature drops sharply when passing through the J-T valve in the subsequent recovery unit, and when the temperature is lower than the freezing and blocking point of benzene, solids are separated out, so that the pipeline is frozen and blocked, and the inventor proposes the technical scheme based on the method. The recovery devices adopted in the following embodiments are all obtained by modifying the existing natural gas medium-pressure cryogenic light hydrocarbon recovery device.
Example 1
According to the benzene-containing natural gas medium pressure cryogenic light hydrocarbon recovery method in the embodiment, the recovery device is formed by connecting a raw gas inlet pipeline of a raw gas buffer tank V01 of the conventional natural gas medium pressure cryogenic light hydrocarbon recovery device (shown in fig. 1) and a top reflux pipeline of a depropanizer T103 through pipelines, and the reformed recovery device is shown in fig. 2 and will not be described again.
The method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon comprises the following steps:
through the connecting pipeline of the top reflux pipe of the depropanizer and the raw gas inlet pipeline of the raw gas buffer tank, part of produced propane product and raw gas are directly mixed (the mass ratio of propane to raw gas is 17:100) and then enter the raw gas buffer tank for buffering, the buffered mixed gas enters a compression unit for pressurizing to 4.5MPa, and then enters a cold box E01 (part of the mixed gas directly enters the cold box E01 and part of the mixed gas enters the cold box E01 after being subjected to heat exchange and cooling by E04) for deep cooling. The gas phase obtained by low-temperature separation returns to the cold box to exchange heat to-80 ℃, then is expanded by an expander to enter a demethanizer T101, and the liquid phase obtained by low-temperature separation returns to the cold box to exchange heat and then flows through a J-T valve to be throttled and cooled to about-101 ℃ to enter the demethanizer. The demethanizer top product is cooled and pressurized by 1.2MPa and then is delivered outwards, and the extract liquid of the tower bottom enters a deethanizer T102 for separation. The deethanizer overhead product is ethane product, which is externally output, and the tower kettle extract enters a depropanizer T103 to separate propane. The depropanizer top product is a propane product, except for the part which is mixed with the raw material natural gas in the raw material gas inlet pipeline of the raw material gas buffer tank V01 before being conveyed to the raw material gas buffer tank V01, the residual propane product is conveyed to a propane storage tank for storage, and the extract liquid of the tower bottom enters a debutanizer T104 to separate butane. The product at the top of the debutanizer is a mixed butane product, the mixed butane product is conveyed to a butane storage tank for storage, the extract liquid at the tower kettle enters a depentanizer T105 for separation, the product at the top of the debutanizer is a mixed pentane product, and the mixed pentane product is conveyed to a pentane storage tank for storage.
According to the embodiment, the top reflux pipeline of the depropanizer is connected with the raw gas inlet pipeline of the raw gas buffer tank, so that the freezing and blocking temperature of the J-T valve can be reduced, and a material flow can enter the depropanizer at a lower temperature, so that the top temperature is reduced, the separation capacity of the depropanizer on methane and ethane is improved, the ethane content in dry gas is reduced, the ethane product yield is improved, and obvious economic and social benefits are created. The mass percentage of benzene in the raw material natural gas is 0.52%, when the mass of propane is 17% of the mass of the raw material natural gas, the temperature of the J-T valve after freezing and blocking is reduced from-101 ℃ to-105.7 ℃, and the process requirement is met.
Example 2
According to the benzene-containing natural gas medium pressure cryogenic light hydrocarbon recovery method in the embodiment, the recovery device is that the raw material gas inlet pipeline of the raw material gas buffer tank V01 of the existing natural gas medium pressure cryogenic light hydrocarbon recovery device (shown in fig. 1) is connected with a propane storage tank and a butane storage tank through pipelines, and the reformed recovery device is shown in fig. 3 and is not repeated here.
The method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon comprises the following steps:
through the raw material gas inlet pipeline of the raw material gas buffer tank V01 and the connecting pipeline of the propane storage tank and the butane storage tank, the stored propane product and butane product are directly mixed with raw material natural gas (the total mass ratio of propane, butane and raw material natural gas mixed in the raw material natural gas is 4:16:100) and then enter the raw material gas buffer tank for buffering, the buffered mixed gas enters the compression unit for pressurizing to 4.5MPa, and then enters the cold box E01 after being dehydrated by the drying unit (part directly enters the cold box E01, and part enters the cold box E01 after being subjected to heat exchange and cooling by E04). The gas phase obtained by low-temperature separation returns to the cold box to exchange heat to-80 ℃, then is expanded by an expander to enter a demethanizer T101, and the liquid phase obtained by low-temperature separation returns to the cold box to exchange heat and then flows through a J-T valve to be throttled and cooled to about-101 ℃ to enter the demethanizer to separate methane. Methane products at the top of the demethanizer are externally conveyed after being cooled and pressurized by 1.2MPa, and the extract liquid at the bottom of the demethanizer enters a deethanizer T102 to separate ethane. The deethanizer overhead product is ethane product, which is externally output, and the tower kettle extract enters a depropanizer T103 to separate propane. The depropanizer top product is a propane product, except for the part which is mixed with the raw material natural gas in the raw material gas inlet pipeline of the raw material gas buffer tank V01 before being conveyed to the raw material gas buffer tank V01, the residual propane product is conveyed to a propane storage tank for storage, and the extract liquid of the tower bottom enters a debutanizer T104 to separate butane. The product at the top of the debutanizer is a mixed butane product, the mixed butane product is conveyed to a butane storage tank for storage, the extract liquid at the tower kettle enters a depentanizer T105 for separating pentane, the product at the top of the debutanizer is a mixed pentane product, and the mixed pentane product is conveyed to the pentane storage tank for storage.
According to the embodiment, the propane of the propane storage tank and the butane of the butane storage tank are mixed with the raw material natural gas in the raw material gas inlet pipeline of the raw material gas buffer tank through the pipeline, so that the freezing and blocking temperature after the J-T valve can be reduced. The mass percentage of benzene in the raw material natural gas is 0.52%, when propane and butane are mixed into the raw material natural gas according to the mass ratio of 1:4, the total mass of the propane and the butane is 20% of the mass of the raw material natural gas, and the temperature at which freezing and blocking occur after the J-T valve is reduced from-101 ℃ to-108.4 ℃ so as to meet the process requirements.
Example 3
According to the benzene-containing natural gas medium pressure cryogenic light hydrocarbon recovery method in the embodiment, the recovery device is that the raw material gas inlet pipeline of the raw material gas buffer tank V01 of the existing natural gas medium pressure cryogenic light hydrocarbon recovery device (shown in fig. 1) is connected with the top reflux pipeline of the depropanizer T103, the pentane storage tank and the butane storage tank through pipelines, and the reformed recovery device is shown in fig. 4 and will not be repeated here.
The method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon comprises the following steps:
the top reflux pipeline, the pentane storage tank and the butane storage tank of the depropanizer are connected with the feed gas inlet pipeline of the feed gas buffer tank through pipelines, part of propane products, stored butane products and stored pentane products produced by the depropanizer are directly mixed with feed natural gas (the mass ratio of propane, butane, pentane and feed natural gas mixed in the feed natural gas is 4:4:12:100) and then enter the feed gas buffer tank for buffering, the buffered mixture enters a compression unit for pressurizing to 4.5MPa, and then enters a cold box E01 (part of the mixture directly enters the cold box E01 after being dehydrated by a drying unit, and the other part of the mixture enters the cold box E01 after being subjected to heat exchange and temperature reduction by E04) for cryogenic cooling. The gas phase obtained by low-temperature separation returns to the cold box to exchange heat to-80 ℃, then is expanded by an expander and enters a demethanizer T101, and the liquid phase obtained by low-temperature separation returns to the cold box to exchange heat and then flows through a J-T valve to be throttled and cooled to about-101 ℃ and enters the demethanizer. Methane products at the top of the demethanizer are externally conveyed after being cooled and pressurized by 1.2MPa, and the extract liquid at the bottom of the demethanizer enters a deethanizer T102 to separate ethane. The deethanizer overhead product is ethane product, which is externally output, and the tower kettle extract enters a depropanizer T103 to separate propane. The depropanizer top product is a propane product, except for the part which is mixed with the raw material natural gas in the raw material gas inlet pipeline of the raw material gas buffer tank V01 before being conveyed to the raw material gas buffer tank V01, the residual propane product is conveyed to a propane storage tank for storage, and the extract liquid of the tower bottom enters a debutanizer T104 to separate butane. The product at the top of the debutanizer is a mixed butane product, the mixed butane product is conveyed to a butane storage tank for storage, the extract liquid at the tower kettle enters a depentanizer T105 for separating pentane, the product at the top of the debutanizer is a mixed pentane product, and the mixed pentane product is conveyed to the pentane storage tank for storage.
According to the embodiment, the propane of the propane storage tank and the butane of the butane storage tank are mixed with the raw material natural gas in the raw material gas inlet pipeline of the raw material gas buffer tank through the pipeline, so that the freezing and blocking temperature after the J-T valve can be reduced. In the embodiment, the mass percentage of benzene in the raw natural gas is 0.52%, when the mass ratio of propane, butane and pentane is 1:1:3, the total mass of the propane, the butane and the pentane is 20% of the mass of the raw natural gas, and the temperature at which freezing and blocking occur after the J-T valve is reduced from-101 ℃ to-113.6 ℃, so that the process requirement is met.

Claims (9)

1. A method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon is characterized in that: the method comprises the following steps: pressurizing raw material natural gas, drying, dehydrating, cryogenic cooling, sending into a low-temperature separator for low-temperature separation, and sending a liquid phase obtained by the low-temperature separation into a dealkylation tower after throttling expansion through a J-T valve; the liquid phase obtained by low-temperature separation before the J-T valve or the raw natural gas upstream of the low-temperature separator is mixed with C3-C5 alkane.
2. The method for recycling the middle-pressure cryogenic light hydrocarbon of the benzene-containing natural gas according to claim 1, which is characterized in that: the mixing amount of the C3-C5 alkane can lead the precipitation temperature of benzene in the material flowing through the J-T valve to be lower than the temperature of the material throttled and expanded by the J-T valve.
3. The method for recovering the middle-pressure cryogenic light hydrocarbon from the benzene-containing natural gas according to claim 1 or 2, which is characterized in that: mixing C3-C5 alkane into the raw material natural gas before pressurization.
4. The method for recovering the middle-pressure cryogenic light hydrocarbon from the benzene-containing natural gas according to claim 3, which is characterized by comprising the following steps: the dealkylation tower is a demethanizer, and the method for recycling the benzene-containing natural gas medium-pressure deep-cooling light hydrocarbon further comprises the following steps: and sending the extracting solution of the tower kettle of the demethanizer into the deethanizer for separating ethane, and sending the extracting solution of the tower kettle of the deethanizer into the depropanizer for separating propane.
5. The method for recycling the light hydrocarbon by deep pressure and deep cooling in the benzene-containing natural gas according to claim 4, which is characterized in that: mixing part of propane separated by a depropanizer into raw natural gas before pressurization;
and/or storing the propane separated from the depropanizer in a propane tank, and transporting the propane in the propane tank to mix into the raw natural gas prior to pressurization.
6. The method for recycling the light hydrocarbon by deep pressure and deep cooling in the benzene-containing natural gas according to claim 4, which is characterized in that: the method also comprises the following steps: and (3) sending the extract of the bottom of the depropanizer into the debutanizer for separating butane.
7. The method for recycling the light hydrocarbon by deep pressure and deep cooling in the benzene-containing natural gas according to claim 6, which is characterized in that: mixing part of butane separated by the debutanizer into raw natural gas before pressurization;
and/or storing butane separated from the debutanizer in a butane storage tank, and transporting butane in the butane storage tank to be mixed into the raw natural gas before pressurization.
8. The method for recycling the light hydrocarbon by deep pressure and deep cooling in the benzene-containing natural gas according to claim 6, which is characterized in that: the method also comprises the following steps: and feeding the extract of the bottom of the debutanizer into a depentanizer for separating pentane.
9. The method for recycling the middle-pressure cryogenic light hydrocarbon of the benzene-containing natural gas according to claim 8, which is characterized in that: mixing part of pentane separated by the depentanizer into raw natural gas before pressurization;
and/or storing the pentane separated from the depentanizer in a pentane storage tank, and transporting the pentane in the pentane storage tank into the raw natural gas before pressurization.
CN202310498337.9A 2023-04-28 2023-04-28 Method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon Pending CN116481261A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116966711A (en) * 2023-08-11 2023-10-31 中工国际工程股份有限公司 Light hydrocarbon recovery system

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116966711A (en) * 2023-08-11 2023-10-31 中工国际工程股份有限公司 Light hydrocarbon recovery system
CN116966711B (en) * 2023-08-11 2024-05-10 中工国际工程股份有限公司 Light hydrocarbon recovery system

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