RU2470865C2 - Method of preparing hydrocarbon gas and apparatus for realising said method - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: invention can be used in gas and oil industry. The apparatus for preparing hydrocarbon gas has a gas separation unit 1, a gas adsorption drying and gasoline extraction unit 2, a hydrocarbon stabilisation unit 3 and a compression unit 4. Unit 1 has separators and is fitted with a separated gas outlet I, a hydrocarbon condensate outlet II and a water outlet III. The gas adsorption drying and gasoline extraction unit 2 has adsorbers filled with silica gel and is fitted with a prepared gas outlet IV which is linked with a booster compressor station 5, a gas outlet V after adsorbent regeneration, a hydrocarbon condensate outlet VI and a water outlet VII. The regeneration gas used in unit 2 is a stream X. Hydrocarbon condensates from outlets II and VI are merged and fed into stabilisation unit 3 which is fitted with a stabilisation gas outlet VIII and an outlet IX for stable condensate, which is the end product. Stabilisation gases are taken for in-house needs or compression in unit 4 and subsequently fed into the stream of starting gas or into the stream of spent gas in outlet V or the stream of prepared gas in outlet IV.

EFFECT: high quality of preparing hydrocarbon gas to obtain additional products, reduced loss of desired hydrocarbon fractions.

3 cl, 4 dwg, 3 ex

Description

The invention relates to techniques and technologies for the preparation of hydrocarbon gas and can be used in gas, oil and other industries on existing and newly designed installations for the preparation and processing of hydrocarbon gases.

A known method for the preparation of hydrocarbon gas, carried out at the gas treatment unit (see RF patent No. 2381822, B01D 53/04, published on 02.20.2010), including the supply of pre-compressed raw gas for separation with removal of the separated hydrocarbon condensate and water, adsorption drying of gas with the removal of the prepared gas, regeneration of the adsorbent with heated gas to obtain, after regeneration, a gas containing water, its cooling and separation with exhaust gas regeneration and water, the supply of exhaust gas reg generation for purification from mechanical impurities and subsequent membrane separation of the regeneration waste gas with retentate and permeate offsets, while the resulting permeate is fed into the crude gas stream before compression.

Common features of the known and proposed methods are:

- gas separation with removal of hydrocarbon condensate and water;

- adsorption drying of gas with the removal of the prepared gas;

- regeneration of the adsorbent with heated gas to obtain, after regeneration, a gas containing water;

- cooling and gas separation after regeneration of the adsorbent with exhaust gas regeneration and water.

The disadvantage of this method is the loss of the target hydrocarbons, which can be used as raw materials for the production of stable gas gasoline or BFLH, due to the discharge into the drain obtained during gas separation of hydrocarbon condensate. In addition, the permeate obtained during membrane separation (part of the regeneration exhaust gas stream containing heavy hydrocarbons and moisture) is sent after compression and separation to adsorption drying of the gas, which leads to an increase in the content of heavy hydrocarbons in the gas and, consequently, to increased coking activity of the sorbent, quality of gas preparation and reducing the service life of the sorbent.

The closest in technical essence and the achieved result to the proposed technical solution is a method of gas treatment (see RF patent No. 2367505, B01D 53/02, B01D 53/26, publ. 09/20/2009), including preliminary gas separation with removal of the separated hydrocarbon condensate and water, adsorption drying and gas topping, removal of the prepared gas, regeneration of the adsorbent with a heated gas to obtain, after regeneration, a gas containing heavy hydrocarbons and water, its cooling and separation with waste heaps for regeneration, hydrocarbon condensate and water, while the regeneration exhaust gas is supplied to the gas stream entering the preliminary separation.

Common features of the known and proposed methods are:

- gas separation with removal of the separated hydrocarbon condensate and water;

- adsorption drying and gas topping;

- removal of prepared gas;

- regeneration of the adsorbent with heated gas to obtain, after regeneration, a gas containing heavy hydrocarbons and water;

- cooling and gas separation after regeneration of the adsorbent with exhaust gas regeneration, hydrocarbon condensate and water.

The disadvantage of this method is the loss of target hydrocarbons With _{3 + above} , which can be used as raw material for the production of stable gas condensate, due to discharge into the drain obtained from the preliminary gas separation of hydrocarbon condensate, which leads to a decrease in production. In addition, due to the regeneration of the adsorbent by a part of the flow of crude gas entering the adsorption drying and topping, the degree of regeneration of the adsorbent and, consequently, the depth of gas preparation are deteriorated.

An object of the invention is to improve the quality of the preparation of hydrocarbon gas, obtaining additionally targeted liquid products — stable gas gasoline or a wide fraction of light hydrocarbons, and reducing / eliminating losses of the target hydrocarbon fractions.

This object is achieved in that in a method for preparing a hydrocarbon gas, including gas separation with discharges of the separated hydrocarbon condensate and water, adsorption drying and gas topping, removal of the prepared gas, regeneration of the adsorbent by heated gas to obtain, after regeneration, a gas containing heavy hydrocarbons and water, its cooling and separation with exhaust gas recovery regeneration, hydrocarbon condensate and water, according to the invention, hydrocarbon condensate separated at gas vaporization and hydrocarbon condensate obtained during cooling and gas separation after regeneration of the adsorbent are subjected to stabilization to obtain stable condensate and stabilization gases, while the liberated stabilization gases are sent for their own needs or for additional compression with subsequent supply or to the source gas stream, or into a regeneration exhaust gas stream, or into a prepared gas stream.

The stabilization of the hydrocarbon condensate separated during gas separation and the hydrocarbon condensate obtained by cooling and gas separation after regeneration of the adsorbent allows the obtained hydrocarbon condensate to be involved in processing in order to generate additional products and thereby eliminate the loss of target C _{3 +} hydrocarbons _above .

The supply of released stabilization gases for their own needs allows the use of the obtained stabilization gases at low pressure.

The flow of stabilized gases for additional compression and further into the flow of the source gas makes it possible to extract additional hydrocarbons during gas topping.

The flow of stabilized gases for additional compression and further into the regeneration exhaust gas stream allows these gases to be used together with the regeneration exhaust gas stream for own needs at a higher pressure (for example, in the fuel system).

The flow of stabilized gases for additional compression and further into the flow of the prepared gas allows these gases to be sent together with the prepared gas to the consumer.

A known installation for the preparation of hydrocarbon gas (see RF patent No. 2381822, B01D 53/04, publ. 02/20/2010), including a separator with a drain of hydrocarbon condensate and water, a unit for adsorption gas drying with a drain of prepared gas and gas after regeneration of the adsorbent, a refrigerator and a chilled gas separator after the regeneration of the adsorbent with exhaust gas regeneration and water, the installation is equipped with a unit for the preparation of exhaust gas regeneration, including a membrane separation unit.

Common features of the known and proposed installations are:

- gas separation unit with removal of hydrocarbon condensate and water;

- a block of adsorption gas drying with taps of prepared gas and gas after regeneration of the adsorbent;

- fridge;

- chilled gas separator after regeneration of the adsorbent with exhaust gas regeneration and water.

A disadvantage of the known installation is the loss of the target hydrocarbon fractions, which can be used as raw materials for the production of stable gas gasoline or BFLH, due to the discharge of hydrocarbon condensate obtained in the gas separation unit into the drain, as well as increased capital and operating costs due to the fact that gas is dried and topped off are carried out at two process plants (gas adsorption dehydration unit and a low-temperature processing unit). In addition, the permeate obtained in the membrane separation unit (part of the regeneration exhaust gas stream containing heavy hydrocarbons and moisture) is sent after the compressor and separator to the adsorption dehydration unit of the gas, which leads to an increase in the content of heavy hydrocarbons in the gas and, consequently, to increased coking of the sorbent , reducing the quality of gas preparation and reducing the service life of the sorbent.

The closest in technical essence and the achieved result to the proposed installation is a gas treatment unit (see RF patent No. 2367505, B01D 53/02, B01D 53/26, publ. 09/20/2009), including a separator with drainage of hydrocarbon condensate and water and a unit adsorption drying and gas topping with vents of prepared gas and gas after regeneration of the adsorbent, refrigerators and a gas separator after regeneration of the adsorbent with vents of regeneration exhaust gas, hydrocarbon condensate and water, while exhaust gas regeneration connected to the supply line of the source gas in front of the inlet separator.

Common features of the known and proposed installations are:

- gas separation unit with removal of hydrocarbon condensate and water;

- block adsorption drying and topping of gas with taps of prepared gas and gas after regeneration of the adsorbent;

- fridge;

- a chilled gas separator after regeneration of the adsorbent with exhaust gas recovery regeneration, hydrocarbon condensate and water.

A disadvantage of the known installation is the loss of the target hydrocarbon fractions, which can be used as raw material for the production of stable gas gasoline and BFLH, due to the discharge of hydrocarbon condensate obtained in the gas separation unit into the drain. In addition, due to the regeneration of the adsorbent by a part of the flow of crude gas entering the adsorption drying and topping, the degree of regeneration of the adsorbent and, consequently, the depth of gas preparation are deteriorated.

An object of the invention is to improve the quality of the preparation of hydrocarbon gas, obtaining additionally targeted liquid products — stable gas gasoline or a wide fraction of light hydrocarbons, and reducing / eliminating losses of the target hydrocarbon fractions.

The problem is achieved in that in the installation of hydrocarbon gas treatment, including a gas separation unit with exhausts of hydrocarbon condensate and water, an adsorption drying and gas topping unit with exhausts of prepared gas and gas after regeneration of the adsorbent, a refrigerator and a chilled gas separator after regeneration of the adsorbent with exhaust gas regeneration, hydrocarbon condensate and water, according to the invention, the removal of hydrocarbon condensate from the gas separation unit and removal hydrocarbon condensate from the chilled gas separator after regeneration of the adsorbent is connected to an additionally installed hydrocarbon stabilization unit, equipped with taps of stabilization gases and stable condensate.

In addition, the stabilization gas outlet is connected to an additionally installed compression unit, the outlet of which is connected either to the source gas stream, or to the outlet of the regeneration exhaust gas, or to the outlet of the prepared gas.

Providing the installation with an additional hydrocarbon stabilization unit, which is connected to the discharge of hydrocarbon condensate from the gas separation unit and to the removal of hydrocarbon condensate from the chilled gas separator after regenerating the adsorbent, allows the resulting hydrocarbon condensate to be recycled in order to generate additional products, thereby eliminating the loss of the target hydrocarbon fractions .

The connection of the stabilization gas outlet to an additionally installed compression unit, the outlet of which is connected either to the source gas stream, or to the outlet of the regeneration exhaust gas, or to the outlet of the prepared gas, allows either to extract additional hydrocarbons during topping, or to use stabilization gases together with the exhaust stream regeneration gas for own needs at high pressure (for example, in the fuel system), or send the obtained stabilization gases together with the preparation ennym gas consumer.

Thus, the claimed combination of features allows through the use of integrated technology to carry out the preparation of hydrocarbon gas to the required standards, as well as to obtain stable gas gasoline or BFLH both in the fields and at the gas processing plant.

Fig. 1 shows a block diagram of a hydrocarbon gas preparation unit, on which the proposed method is implemented, Fig. 2 shows a block of adsorption drying and gas topping, Fig. 3 shows a block of hydrocarbon stabilization С _{3 + above} , and Fig. 4 shows a block stabilization of hydrocarbons With _{5 + above} .

The installation contains (see Fig. 1) a gas separation unit 1 with a branch I of separated gas, a branch II of hydrocarbon condensate and a branch of III water. Block 1 consists of one or more separators of different pressure levels (not shown).

Outlet I is connected to the adsorption drying and gas stripping unit 2, equipped with an outlet IV for prepared gas, an outlet V for regeneration exhaust gas, an outlet VI for hydrocarbon condensate and an outlet for water VII.

The installation is equipped with an additional block 3 of hydrocarbon stabilization with a vent of VIII stabilization gases and a vent of IX of the target liquid products and a compression unit 4.

The installation can be equipped with a booster compressor station 5 (DKS).

Block 2 (see Fig. 2) consists of adsorbers 6-8 filled with silica gel (domestic or imported), which has a sufficient capacity both for water and for C _{3 +} hydrocarbons _above . The top of the adsorbers is connected to the gas supply line I from block 1, the cooling gas exhaust line and the gas exhaust line after the regeneration of the adsorbent, and the bottom - to the prepared gas exhaust line IV, the cooling gas supply line X and the regeneration gas supply line X. Adsorbers 6- 8 operate periodically in the cycles of adsorption - regeneration - cooling. A filter 9 is installed on the vent line IV of the prepared gas from adsorbers 6-8. A filter 10, a recuperative heat exchanger 11, a cooler 12 and a chilled gas separator 13 after the regeneration of the adsorbent are sequentially installed on the gas exhaust line after the adsorbent is regenerated from the adsorbers 6-8. The separator 13 is equipped with a tap V of the exhaust gas regeneration, tap VI of the hydrocarbon condensate and tap VII of the water. The cooling gas removal line from the adsorbers 6-8 is connected in series with the filter 14, a regenerative heat exchanger 11, and the furnace 15.

The outlet IV of the prepared gas from block 2 is connected to the line X of block 2 (see Fig. 1, 2).

The outlet II of hydrocarbon condensate from block 1 and the outlet VI of hydrocarbon condensate from block 2 are connected to block 3 of hydrocarbon stabilization (see Fig. 1).

Hydrocarbon stabilization unit 3 (depending on production

if necessary) can be made in the form of a stabilization block С _{3 + above} (see Fig. 3), including a heat exchanger 16, a distillation column 17 with an irrigation unit for the top of the column, consisting of an air cooler 18, a separator 19 and a pump 20, and heated bottom of the column a reboiler 21, or stabilization block C _{5 + above} (see Fig. 4), which includes a heat exchanger 22, separators 23, 24, a pump 25 and a heat exchanger 26 installed in series. As a stabilization block C _{3 + above} or a stabilization block C _{5 + above} any other known installation scheme may be applied stabilization.

The outlet of the VIII stabilization gases from block 3 can be connected to an additional compression block 4 (see Fig. 1).

The output from the compression unit 4 can be connected either to the source gas stream in front of the unit 1, or to the outlet V of the regeneration exhaust gas, or to the outlet IV of the prepared gas (see Fig. 1).

The proposed method is carried out on the installation as follows.

Hydrocarbon gas with a pressure of 0.8 MPa or more and a temperature of 20 ... 40 ° C is supplied to the gas separation unit 1, in which gas I is separated from hydrocarbon condensate II and water III. After separation, gas I enters the adsorption drying and gas topping unit 2, hydrocarbon condensate II is sent to the hydrocarbon stabilization unit 3, and the released water III is discharged from the unit and discharged into the drain.

In block 2, gas is dried and stripped on an adsorbent, for example, BASF silica gel. Prepared gas IV with a pressure of at least 0.4 MPa (g) is removed from block 2 and sent to the consumer or (if necessary) to DCS 5. After completion of the adsorption cycle, adsorbers 6-8 are transferred to a regeneration and further cooling cycle.

As a regeneration and cooling gas, a part of the prepared gas stream IV is used (see Fig. 1, 2, stream X). The gas is heated in the furnace 15 to a temperature of 160 ... 280 ° C and sent to the adsorber 6-8, switched into the regeneration cycle. During regeneration, absorbed heavy hydrocarbons and water are extracted from the adsorbent. After the regeneration, the gas containing heavy hydrocarbons and water is cooled in the recuperative heat exchanger 11 and the refrigerator 12 and then enters the chilled gas separator 13 after regenerating the adsorbent, in which the heavy hydrocarbons and water are separated, followed by the exhaust of the regeneration exhaust gas V, hydrocarbon condensate VI and water VII, after which the exhaust gas of regeneration V is sent for own needs, hydrocarbon condensate VI is sent to block 3 of hydrocarbon stabilization, and ode VII derived from the plant.

In block 3 of hydrocarbon stabilization, which receives hydrocarbon condensate II from block 1 and hydrocarbon condensate VI from block 2, stabilization gases VIII are released and the desired liquid products IX are obtained - fractions C _{3 + higher} (wide fraction of light hydrocarbons) or C _{5 + higher} (stable gas gasoline). The obtained stabilization gases VIII, depending on the need, can be sent to own needs or for additional compression to block 4 with subsequent supply to either the source gas stream before block 1, or to the regeneration exhaust gas stream V, or to the prepared gas stream IV.

Example 1

Hydrocarbon gas with a pressure of 6.4 MPa and a temperature of 20 ... 40 ° C in an amount of 43000 ... 44000 nm ³ / h with a C _{3 +} content _{higher than} 100 g / m ³ is fed to gas separation unit 1 to separate gas I from hydrocarbon condensate II c the amount of 200 ... 220 kg / h and water III. After separation, the separated gas I enters the adsorption drying and gas topping unit 2, and the resulting hydrocarbon condensate II is sent to the hydrocarbon stabilization unit 3. The water III released in block 1 is discharged from the installation and discharged into the drainage.

In block 2, adsorption drying and gas topping occurs on BASF silica gel. Prepared gas IV with a dew point temperature of water minus 20 ... 40 ° C and hydrocarbons minus 10 ... minus 30 ° C in an amount of 41,000 ... 42,000 nm ³ / h and a pressure of at least 6.1 ... 6.3 MPa (g) leaves block 2 and is sent to the consumer.

After the completion of the adsorption cycle, the adsorbers 6-8 are transferred to the regeneration cycle and further cooling.

As the regeneration gas, a part of the prepared gas stream IV (stream X) is used in an amount of 3400 ... 4400 nm ³ / h. The gas is heated in the furnace 15 to a temperature of 160 ... 280 ° C and sent to the adsorber switched into the regeneration cycle. During regeneration, absorbed heavy hydrocarbons and water are extracted from the adsorbent. After the regeneration, the gas containing heavy hydrocarbons and water is cooled in the recuperative heat exchanger 11, the refrigerator 12 and separated in the chilled gas separator 13 after regeneration of the adsorbent, while the regeneration exhaust gas V is discharged from the separator 13 in an amount of 1700 ... 1800 nm ³ / h hydrocarbon condensate VI in the amount of 1300 ... 2200 kg / h and water VII in the amount of 45 ... 60 kg / h, after which the exhaust gas of regeneration V is sent to its own needs, water VII is removed from the installation, and the resulting hydrocarbon condensate Nsat VI is combined with hydrocarbon condensate II from block 1 and sent to block 3 of hydrocarbon stabilization.

Block 3 products are stable condensate IX in the amount of 1440 ... 2320 kg / h and stabilization gases VIII in the amount of 0 ... 100 nm ³ / h. Received stabilization gases VIII are sent to their own needs.

Example 2

Hydrocarbon gas with a pressure of 6.0 MPa and a temperature of 20 ... 40 ° C in an amount of 5700 ... 57,500 nm ³ / h with a C 3+ content _above 100 g / m ³ is fed to gas separation unit 1 to separate gas I from hydrocarbon condensate II c the amount of 60 ... 100 kg / h and water III. After separation, the separated gas I enters the adsorption drying and gas topping unit 2, and the resulting hydrocarbon condensate II in the amount of 120 ... 130 kg / h is sent to the hydrocarbon stabilization unit 3. The water III released in block 1 is discharged from the installation and discharged into the drainage.

In block 2, adsorption drying and gas topping occurs on BASF silica gel. Prepared gas IV with a dew point temperature of water minus 20 ... 40 ° C and hydrocarbons minus 10 ... minus 30 ° C in an amount of 56900 ... 556950 nm ³ / h and a pressure of at least 5.8 ... 5.9 MPa (g) leaves block 2 and is sent to the consumer.

After the completion of the adsorption cycle, the adsorbers 6-8 are transferred to the regeneration cycle and further cooling.

As the regeneration gas, a part of the prepared gas stream IV (stream X) is used in an amount of 3310 ... 3350 nm ³ / h. The gas is heated in the furnace 15 to a temperature of 160 ... 280 ° C and sent to the adsorber switched into the regeneration cycle. During regeneration, absorbed heavy hydrocarbons and water are extracted from the adsorbent. After the regeneration, the gas containing heavy hydrocarbons and water is cooled in the recuperative heat exchanger 11, the refrigerator 12 and is separated in the chilled gas separator 13 after regeneration of the adsorbent, while the exhaust gas of regeneration V in the amount of 3390 ... 3400 nm ³ / h is removed from the separator 13 , hydrocarbon condensate VI in the amount of 45 ... 46 kg / h and water VII in the amount of 45 ... 60 kg / h, after which the exhaust gas of regeneration V is directed to its own needs, water VII is removed from the installation, and the resulting hydrocarbon condens At VI is combined with hydrocarbon condensate II from block 1 and sent to block 3 of hydrocarbon stabilization.

Block 3 products are stable condensate IX in an amount of 160 ... 170 kg / h and stabilization gases VIII in an amount of 0 ... 100 nm ³ / h.

The resulting stabilization gases VIII are combined with exhaust gas regeneration V and sent to their own needs.

Example 3

Hydrocarbon gas with a pressure of 2.0 ... 6.0 MPa and a temperature of 20 ... 40 ° C in an amount of 119000 ... 120,000 nm ³ / h with a density of 0.79 kg / m ³ is supplied to gas separation unit 1 for separating gas I from hydrocarbon condensate II in the amount of 350 ... 400 kg / h and water III. After separation, the separated gas I enters the adsorption drying and gas topping unit 2, and the resulting hydrocarbon condensate II is sent to the hydrocarbon stabilization unit 3. The water III released in block 1 is discharged from the installation and discharged into the drainage.

In block 2, adsorption drying and gas topping occurs on BASF silica gel. Prepared gas IV with a dew point temperature of water minus 20 ... minus 40 ° C and hydrocarbons minus 10 ... minus 30 ° C in an amount of 118500 ... 119500 nm ³ / h and a pressure of at least 2.0 MPa (g) leaves the unit 2 and sent to the consumer.

After the completion of the adsorption cycle, the adsorbers 6-8 are transferred to the regeneration cycle and further cooling.

As the regeneration gas, a part of the prepared gas stream IV (stream X) is used in an amount of 12000 ... 14000 nm ³ / h. The gas is heated in the furnace 15 to a temperature of 160 ... 280 ° C and sent to the adsorber switched into the regeneration cycle. During regeneration, absorbed heavy hydrocarbons and water are extracted from the adsorbent. After the regeneration, the gas containing heavy hydrocarbons and water is cooled in the recuperative heat exchanger 11, the refrigerator 12 and is separated in the chilled gas separator 13 after the regeneration of the adsorbent, while the exhaust gas regeneration V in the amount of 12000 ... 14000 nm ³ / h is removed hydrocarbon condensate VI in the amount of 700 ... 900 kg / h and water VII in the amount of 45 ... 60 kg / h, after which the exhaust gas of regeneration V is directed to its own needs, water VII is removed from the installation, and the resulting hydrocarbon condensate Nsat VI is combined with hydrocarbon condensate II from block 1 and sent to block 3 of hydrocarbon stabilization.

Block 3 products are stable condensate IX in the amount of 900 ... 1300 kg / h and stabilization gases VIII in the amount of 10 ... 200 nm ³ / h. The resulting stabilization gases VIII are sent to the reception of the COP in the compression unit 4.

Further, depending on the technological need, compressed stabilization gases with a pressure not lower than the source gas pressure (0.8 MPa) can be connected to the source gas stream in front of block 1, which will allow additional hydrocarbons to be extracted during topping (140-200 kg / h )

Compressed stabilization gases with a pressure of 1.6-4.0 MPa can be connected to the exhaust gas stream of regeneration V and directed to own needs in the fuel system.

In addition, the compressed stabilization gases with a pressure of 1.6-4.0 MPa can be connected to the stream of prepared gas IV and then sent to the consumer or to DCS 5.

Claims (3)

1. A method of preparing hydrocarbon gas, including gas separation with drains of the separated hydrocarbon condensate and water, adsorption drying and gas topping, removal of the prepared gas, regeneration of the adsorbent by heated gas to obtain, after regeneration, a gas containing heavy hydrocarbons and water, cooling and separation thereof exhaust gas recovery regeneration, hydrocarbon condensate and water, characterized in that the hydrocarbon condensate separated during gas separation, and hydrocarbon condensate, obtained by cooling and gas separation after regeneration of the adsorbent, is subjected to stabilization to obtain stable condensate and stabilization gases, while the liberated stabilization gases are sent for their own needs or for additional compression, followed by supply to either the source gas stream or the regeneration exhaust gas stream, or into a stream of prepared gas. 2. Installation for the preparation of hydrocarbon gas, including a gas separation unit with taps of hydrocarbon condensate and water, an adsorption drying and gas topping unit with taps of prepared gas and gas after regenerating the adsorbent, a refrigerator and a chilled gas separator after regenerating the adsorbent with exhaust taps of regeneration, hydrocarbon condensate and water, characterized in that the removal of hydrocarbon condensate from the gas separation unit and the removal of hydrocarbon condensate from the separator chilled gas after regeneration of the adsorbent is connected to an additionally installed hydrocarbon stabilization unit, equipped with vents of stabilization gases and stable condensate. 3. The hydrocarbon gas preparation unit according to claim 2, characterized in that the stabilization gas outlet is connected to an additionally installed compression unit, the outlet of which is connected either to the source gas stream, or to the outlet of the regeneration exhaust gas, or to the outlet of the prepared gas.

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