EA025118B1 - Flareless condensate stabilization in combination with gas conditioning - Google Patents

Abstract

The invention relates to a processing scheme for gas conditioning, comprising an expansion-coolingbased separation stage (200) and a stabilisation stage (300). The expansion-coolingbased separation stage (200) comprises an expander (EXP), a separator (SEP) and a compressor (COM), and is arranged to receive an input stream (I2). The stabilisation stage (300) comprises a fractionation column (FC), and is arranged to receive an intermediate input stream (I3) from the expansion-coolingbased separation stage (200). The processing scheme further comprises a jet pump (JP), arranged to receive at least part of a fractionation top stream (FT) and a portion of the input stream (I2') taken upstream of the expander (EXP), to combine these into a feedback stream (FS) which is re-introduced in the expansion-coolingbased separation stage (200) at a feedback position.

Description

The invention relates to a method and system for gas conditioning.

State of the art

Dew point control and condensate stabilization are common practice in the gas and oil industries. Water and hydrocarbons are extracted from gas to meet pipeline specifications that are relevant to the national distribution system, or to create an additional revenue item. These factors, combined with the available technology, have led to a huge variety of gas conditioning technology schemes and condensate stabilization technology schemes for gas processing companies. Hydrocarbon dew point control schemes can be based on the following technologies: adsorption and / or refrigerant cooling and / or expansion cooling.

Adsorption is mainly used to simultaneously remove water and hydrocarbons from depleted high-pressure gas streams.

Refrigerant cooling is mainly used at low pressures. A cooling agent is used to cool the gas and thereby the condensation of hydrocarbons.

In the most common expansion expansion, a Joule-Thomson control valve is used. Joule-Thompson cooling is a less efficient isoanthalpic cooling that violates the existing pressure conditions, so re-compression does not occur.

For more efficient cooling, an isentropic expansion can be used, such as in a turboexpander or cyclone separator, such as described in patent document UO 03 / 029739A2. Both include phase expansion and re-compression.

The resulting condensate from all of the above technologies can subsequently be stabilized or withdrawn as an unstable condensate. To stabilize the condensate, light hydrocarbons that are dissolved in the condensate must be removed. This can be achieved either by reducing the pressure to atmospheric and thereby explosive evaporation of liquids in several blocks, or by stripping light gas fractions from liquids using a stabilization column. The stabilization column operates at slightly higher pressures than the explosive evaporation tank, but requires heat to be removed to remove light hydrocarbons from the liquid.

The removed light hydrocarbons can be flared or re-combined with the main process gas stream. As a result of burning, a valuable product is lost and there are CO ₂ emissions. In many countries, they are switching to a torchless technique.

To combine light hydrocarbons with the main process gas stream, it is necessary to re-compress the off-gas using an off-gas compressor unit, since blasting tanks or stabilization columns usually operate at relatively low pressures.

SUMMARY OF THE INVENTION

The aim of the present invention is to provide a circuit system that does not use flaring and additional installations for re-compression or the like.

This goal is achieved by creating a gas conditioning system comprising a separation unit based on expansion cooling, comprising an expander and a separator and adapted to receive an inlet stream that is part of the incoming gas stream, a stabilization unit containing a distillation column and configured to accept an intermediate flow from the separation unit, based on expansion cooling, and a jet pump, one inlet of which is connected to the upper outlet of the distillation column it is, and the second input is designed to accept the input stream, which is another part of the incoming gas stream, and the output of the jet pump is connected to the separation unit for directing the return feed stream into it.

Preferably, the expander of the separation unit based on expansion cooling is configured to expand and adiabatically cool the inlet stream so that at least a portion of the initially gaseous components become supersaturated and form droplets of liquid in the gaseous fluid, and the separator is configured to accept at least part of the expanded flow from the expander, and the separator contains at least one separation tank designed to form the upper stream and the lower stream.

Preferably, the intermediate stream from the separation unit based on expansion cooling is a bottom stream.

Preferably, the stabilization unit further comprises a coagulator and a heat exchanger, wherein the coagulator is designed to receive an intermediate stream and create an overhead stream that is heated by the heat exchanger before being sent to the distillation column.

Preferably, the distillation column is configured to separate at least a portion of the intermediate stream and create a fractionated overhead stream and a fractionated bottom stream.

Preferably, the pressure of the return feed stream is between the pressure of the fractionated 1,025118 overhead stream and the inlet stream and is equal to or greater than the pressure in the insertion position of the return feed stream.

Preferably, the expansion cooling based separation unit comprises a cyclone fluid separator or a Joule-Thomson valve and a separation tank including an expander and a separator.

Preferably, the system further comprises a compressor for increasing the pressure of the return feed stream, wherein the position for introducing the return feed stream is upstream of the expander.

Preferably, the introduction position of the return feed stream is halfway to the expander.

Preferably, the expansion cooling-based separation unit comprises a cyclone fluid separator having a casing in which the central housing is arranged to form an annular gap between the inner surface of the casing and the outer surface of the central housing and creating a tapering fluid inlet section, the cyclone separator for fluid is intended to facilitate the passage of the main stream through the tapering inlet section, and the Central housing contains a Central outlet a channel for introducing a Central stream into the main stream, and the Central exhaust channel forms the position of the introduction of the return feed stream.

Preferably, the introduction position of the return feed stream is located on a separation tank.

Preferably, the expansion-based separation unit comprises a turbo-expander implementing an expander, a separation tank implementing the separator, and a compressor implementing the compressor.

Preferably, the introduction position of the return feed stream is located at the inlet to the separation tank.

Preferably, the introduction position of the return feed stream is downstream of the separation tank and downstream of the compressor.

Preferably, the system further comprising a pre-separation unit comprising at least one separation tank and a heat exchanger and configured to receive an inlet gas stream cooled in the heat exchanger and separate the inlet gas stream by at least one separation tank to form a gas-rich outlet stream and a liquid enriched outlet stream, the gas enriched outlet stream being an inlet stream.

This goal is also achieved by creating a method of conditioning the gas using a system that accepts a fractionated overhead stream and a portion of the inlet stream taken upstream of the expander to combine these streams into a return feed stream, according to which the inlet stream is fed to a cooling-based separation unit an extension in which an intermediate stream is formed; supplying an intermediate stream to a distillation column of a stabilization unit; create a fractionated upper stream and a fractionated lower stream in a distillation column; supplying at least a portion of the fractionated overhead stream and a portion of the inlet stream, taken downstream to the expander, to a jet pump to combine the two streams into a return feed stream; repeatedly from the jet pump to the separation unit, based on expansion cooling, the return feed stream is introduced either into the expander, or upstream to the expander, or downstream after the expander.

Brief Description of the Drawings

The following embodiments of the invention are described by way of example only with reference to the accompanying schematic drawings, in which corresponding reference numbers indicate corresponding parts and which show the following:

FIG. 1 schematically depicts a system according to one embodiment; FIG. 2a-2b — blocks based on expansion cooling; FIG. 3-6 - systems according to options for execution.

DETAILED DESCRIPTION OF THE INVENTION

Presented embodiments include a separation unit 200 based on expansion cooling. This separation unit 200 may be preceded by a preliminary separation unit 100, and a stabilization unit 300 may be provided downstream of it. FIG. 1 shows a schematic view of such a separation system, which will be described in more detail below.

The principle of operation of the separation unit 200, based on expansion cooling, is based on the rapid expansion of the fluid, which is accompanied by a decrease in pressure and thereby cooling and condensation of the initially gaseous components, creating droplets of liquid. Liquid droplets can be separated from the rest of the fluid. After expansion, the fluid may be re-compressed.

Such a separation unit 200 may include an EXP expander, a §EP separator, and possibly a COM compressor. In general, expansion cooling-based separation unit 200 is designed to receive an input stream of gaseous fluid, expand, and thereby adiabatically cool the input stream in an expander, so that at least a portion of the initially gaseous components become supersaturated and condense to form liquid droplets in gaseous fluid, accepting at least a portion of the expanded flow in a separator containing at least one separation tank designed to the formation of the top stream and bottoms stream, and re-compression in the compressor at least part of the incoming input stream after expansion.

The separation vessel may be a liquid degassing vessel, such as, for example, a gravitational separation vessel, a filter separation vessel or a centrifugal separation vessel, or any suitable type separation vessel.

The expansion cooling-based separation unit 200 may further include separators, such as separation tanks, and the like. The EXP expander, 8EP separator, and COM compressor can be used in various ways, some examples of which will be given below with reference to FIG. 2a-2b, respectively, showing a cyclone fluid separator, an alternative embodiment of a cyclone fluid separator, a turboexpander compressor, and a Joule-Thomson pressure reducing valve or valve.

Τν cyclone separator for fluid.

The recovery of gas condensate liquids from natural gas is a common practice in the oil and gas industry. These liquids are recovered to create added value or due to certain technical conditions that must be met. FIG. 2a schematically shows a cyclone fluid separator Τν that can be used on expansion cooling-based separation units 200.

Patent Document νθ 03 / 029739A2 describes a cyclone separator including a tubular neck portion in which a fluid stream is accelerated, possibly to a supersonic speed, and is rapidly cooled as a result of adiabatic expansion. Rapid cooling will cause condensation and / or solidification of the condensed vapors in the fluid stream to form small droplets or particles. If the fluid stream is a natural gas stream leaving a production well for natural gas production, then the condensable vapors may include water, hydrocarbons, carbon dioxide, hydrogen sulfide and mercury. In addition, these separators include an assembly of swirl vanes in the inlet portion upstream of the neck portion, the blade or vanes tilted or spiraling about the central axis of the neck portion to create a swirling movement of the fluid flow inside the separator. Centrifugal forces excited by swirling movement in a fluid mixture will involve condensed and / or hardened relatively high density components in a swirl movement to the outer periphery of the inside of the neck portion and the expanding outlet section, while gaseous components with relatively low density are concentrated near the central axis separator.

The gaseous components are subsequently discharged from the cyclone separator through the primary central outlet, while the condensate-rich fluid stream is removed from the cyclone separator through a secondary outlet, which is located on the outer perimeter of the expanding outlet. A more detailed description of the cyclone separator is given below.

As one example of FIG. 2a is a longitudinal sectional view of a fluid separator, which may also be referred to as a cyclone separator, a cyclone inertial separator, a cyclone fluid separator.

In FIG. 2a shows a cyclone inertial separator, which includes a vortex inlet device having a pear-shaped central body 1, on which swirl blades 2 are mounted and which is located coaxially with the central axis I of the cyclone separator inside the cyclone separator so as to create an annular gap 3 between the central body 1 and casing 20 of the separator.

The width of the annular gap 3 is chosen so that the cross-sectional area of the annular gap gradually decreases downstream relative to the swirl blades 2, so that during application, the flow rate of the fluid in the annular gap gradually increases and reaches supersonic speed in the place downstream relative to the swirl blades 2.

The cyclone fluid separator further includes a tubular neck portion 4, from which, during use, a swirling fluid stream is discharged into an expanding fluid separation chamber 5, which is equipped with a central primary outlet pipe 7 for gaseous components and an external secondary outlet pipe 6 for fluid enriched in condensable components. The central body 1 has a substantially cylindrical elongated end section 8 on which the assembly of the flow-straightening vanes 19 is mounted. The central body 1 has the largest external width or diameter 2K _max , which is larger than the smallest internal width or diameter 2K _PT1P

- 3 025118 diameter of 2H _max , which is larger than the smallest internal width or diameter of 2K _{|| t |||} tubular neck portion 4.

The tubular neck portion 4 includes a portion of an annular gap 3 having the smallest cross-sectional area. The maximum diameter of the central body 1 is larger than the minimum diameter of the tubular neck portion 4.

The various components of the cyclone separator as shown in FIG. 2a.

Swirl vanes 2, which are oriented at an angle (α) relative to the central axis I, circulate the fluid flow. Angle α can vary between 20 and 60 °. Then, the fluid flow is directed into the annulus 3. The cross sectional area of the gap is defined as ² _) ^ gppeg / ^A · appi1iz ^{'n (H H} oi1eg 1D

The last two members are the outer radius and the inner radius of the annular channel at the selected location. The average radius of the annular gap is defined as

Ie.X | 1/2 (N.- e '

At the maximum value of the average radius H _teap , _max , the fluid flow flows between the assembly of the swirling blades 2 with speed and, moreover, the blades deflect the flow direction of the fluid flow in proportion to the deviation angle (α), and so the tangential velocity component is obtained, which is equal to υ _φ = υ · δίη (α), and the axial component of the velocity is _x = u-co8 (a).

The annulus 3 downstream of the swirl imparting vanes 2 swirled fluid stream is expanded to high velocities, wherein the mean radius of the cross section of the annular gap gradually narrowing from N _{TEAP, max} to H _{TEAP, S1G.}

During this annular expansion of the flow, the following two processes occur:

(1) the heat or enthalpy (s) of the flow decreases by the value of Dj = -1 / 2 and ² , thereby causing the condensation of those components of the flow that first reach phase equilibrium, which leads to a swirling emulsion regime of a two-phase flow containing small droplets or solid particles;

(2) the tangential component of the velocity υφ increases inversely with the average radius of the annular gap, mainly in accordance with the equation ^υ φ ^υ φ ^, ι μιιιηΙ · ^(H teap, max ^{/ H} teap, m1n ⁾ .

This leads to a sharp increase in the centrifugal acceleration (a _c ) of the fluid particles, which will ultimately be of the order of ac = (υφ

)

φ.Ι'ίΜΗΐ ^{/ N} theap, t1p,

In the tubular neck portion 4, further expansion to higher fluid flow rates can be provided, or a substantially constant speed can be maintained. In the first case, condensation continues continuously, and the mass of particles will increase. In the latter case, condensation almost ceases after a certain period of relaxation. In both cases, the action of centrifugal forces causes the particles to move to the outer perimeter of the flow section adjacent to the inner wall of the separator casing 20, which is called the separation zone. The period of time during which the particles move to this outer perimeter of the flow section determines the length of the tubular neck portion 4. It is understood that the particles can include solid or solidified particles.

Downstream of the relatively tubular neck portion 4, the wet fluid enriched in condensable components tends to concentrate near the inner surface of the expandable separation chamber 5 for the fluid, and the dry fluid with gaseous components concentrates on or near the central axis I, after which the wet fluid the medium enriched with condensable components is discharged into the external secondary fluid outlet 6 through a single groove or a series of grooves, (micro) pores true sections, while dry gaseous components are discharged into the central primary fluid outlet 7.

In the expanding primary fluid outlet 7, the fluid stream is further braked so that the residual kinetic energy is converted to potential energy.

The expanding primary exhaust pipe may be equipped with an assembly for rectifying the flow of the device, such as rectifying the flow of the blade 19, to utilize the circulation energy.

The term fluid is used to refer to a liquid, a gas, and combinations thereof. Fluids may also contain solid particles.

Swirl vanes 2 can be replaced with other suitable devices that impart a twisting motion. For example, swirl vanes 2 can be formed so as to create a tangential flow of fluid.

Rectifying blades 19 can be replaced by other suitable devices,

- 4,025118 rectifying the current.

The cyclone fluid separator mainly has rotational symmetry about the central axis I.

It should be emphasized that the cyclone separator described above is only an example, and the embodiments described below can also be used in other types of cyclone separators, such as the separator described with reference to patent document AO 0023757.

The cyclone fluid separator TA as described and shown in FIG. 2a can be applied to high pressure flows, i.e. the pressure immediately upstream of the central body may typically be 100 bar (10 MPa).

The cyclone fluid separator shown in FIG. 2a may be applied to an expansion cooling unit 200.

The expander can be formed by an annular gap 3 downstream of the swirl blades 2 up to the expanding separation chamber 5 for the fluid, including the tubular neck portion 4. The separator 8EP can be formed by a separation chamber 5 for the fluid. The COM compressor may be formed by an external secondary fluid outlet 6 and a central primary fluid outlet 7. These parts are shown schematically in FIG. 2a.

Cyclonic fluid separator TA 'with additional central flow.

FIG. 2b schematically depicts an alternative cyclone fluid separator TA that can be applied to expansion cooling separation units 200.

FIG. 2b shows a cross-sectional view of a fluid separator according to one embodiment. The same reference numbers are used to indicate the same parts as above. A pear-shaped central body 10 is used on which swirl blades are mounted 2. The central body 10 is arranged coaxially with the central axis I of the fluid separator inside the separator so that an annular gap 3 is created between the central body 10 and the separator. The fluid flow entering the fluid separator media through this annular gap is called the main flow. The fluid separator further includes a tubular neck portion 4, an expanding fluid separation chamber 5, which is equipped with a central primary outlet 7 for gaseous components, and an external secondary fluid outlet 6, enriched with condensable components.

According to this embodiment, the central body 10 does not include a substantially cylindrical elongated end section 8, as in FIG. 2a. Instead, the central body 10 includes a central outlet channel 13. The central outlet channel 13 is located on the downstream side relative to the central body 10 and is directed toward the neck portion 4. The position and direction of the central outlet channel 13 substantially coincide with the central axis I. The central outlet channel 13 is for introducing a central stream into the cyclone fluid separator 1.

Thus, according to this embodiment, a fluid separator is provided comprising a neck portion 4 located between a tapering fluid inlet section and an expanding fluid outlet section, wherein the expanding fluid outlet section includes an internal primary outlet 7 for a fluid depleted in condensable components, and an external secondary outlet 6 for a fluid enriched in condensable components, and a central housing 1 0 located upstream of the neck portion 4 in the fluid inlet section and disposed substantially coaxially with the central axis I of the fluid separator, the fluid separator being designed to facilitate the flow of the main stream through the tapering fluid inlet section and neck portion 4 toward an expanding fluid outlet section, the central body 10 including a central exhaust channel 13 directed toward the tubular neck portion 4, etc. dnaznachenny for introducing a central flow towards the throat portion 4. The central outlet channel 13 situated upstream of the neck part 4.

The channel 12 can be used to direct the flow of fluid into the Central outlet channel 13.

In use, the central stream substantially coincides with the central axis I and is surrounded by the main stream. The central stream may be a swirling stream.

The central fluid stream created by the central outlet channel 13 ensures the stability of the main stream throughout the fluid separator TA '. The central flow plays a role similar to the substantially cylindrical elongated end section 8 described above with reference to FIG. 2a, in the sense that the central flow prevents disturbance of the vortex movement on the central axis of the main flow.

Since the central stream is not a rigid object (like end section 8) and moves in the same direction as the main stream, friction between the central stream and the main stream

- 5,025,118 is relatively low. This increases the performance of the fluid separator.

According to one embodiment, the fluid separator includes a swirl device 2 for creating a swirling movement of the main stream, at least within the part of the fluid separator T ^ '. An example of such a swirl device is swirl vanes 2 shown in FIG. 2b and described above with reference to FIG. 2a.

The central body 1 may have a substantially circular shape in the direction transverse to the axis and upstream of the swirl device 2 and includes a nose section whose diameter is gradually increased so that the degree of increase in diameter gradually decreases in the downstream direction, and the central body 10 is lower downstream of the swirl device further includes a section whose diameter is gradually reduced in the downstream direction. This is shown in FIG. 2b, depicting a substantially pear-shaped central body 10.

The fluid separator T ^ 'may include a housing 20 in which the central housing 10 is arranged such that an annular gap 3 is created between the inner surface of the housing 20 and the outer surface of the central housing 10.

The fluid separator T ^ 'may include a central outlet 13, which has a swirl device to create a swirling movement of the central stream within at least a portion of the fluid separator (not shown). The turbulence imparted to the central flow may be less than the turbulence of the main flow (i.e., with fewer revolutions per second or fewer revolutions per distance along the path in the direction of the central axis I, so that the vortex motion of the central flow does not break) . By imparting a swirling motion to the central stream, the velocity gradient is reduced tangentially between the central stream and the main stream.

For example, the input velocity in the axial (i.e. longitudinal) direction of the central flow is relatively low, typically 20 m / s, and 0-20 m / s in the tangential direction, while at this point the main flow velocity is high, even, possibly still subsonic, for example, 250 m / s in the axial direction and 100 m / s in the tangent. However, the main flow at this point may already be supersonic.

Therefore, the amount of movement of the central stream will be stimulated by the external main stream both in the axial and in the tangential direction (similar to the principle of the jet pump / gas ejector). The function of the end section 8 (i.e., the prevention of additional tangential acceleration causing the destruction of the vortex) is replaced by a gaseous central stream. Instead of the friction-induced scattering of the pulse at the boundary of the elongated end portion 8, part of the momentum of the main stream is used (i.e. transferred) to stimulate the central gas stream.

Between the casing 20 and the central body 10 for attaching the central body 10, a series of bars 21 can be arranged. The bars 21 can be placed upstream of the swirl device 2 so that the bars 21 have less impact on the main flow. According to one alternative embodiment, the swirl device 2 and the crossbeams 21 are combined into a single integral part. In addition, one or more rungs 21 can be hollow and connected to the flow channel 12 as a flow guide to the central outlet channel 13.

In FIG. 2b shows three pressure symbols: P0, P1 and P2. P0 represents upstream pressure relative to the central body 10 and can typically be of the order of 100 bar (10 MPa). P1 represents the pressure in the position of the central outlet channel 13 and typically may be 50-70% lower than P0. P2 represents the pressure in the position of the secondary exhaust pipe 6 and typically may be 25-50% lower than the inlet pressure P0. It will be understood that the pressures P0, P1 and P2 may vary depending on the pressure supplied to the separator T ^ 'for the fluid and the actual shape of the separator T ^' for the fluid and the central housing 10. However, the following relationship is usually observed: P0 > P2> P1.

Thus, in the process of application, the central outlet channel 13 is at the first pressure P1 (i.e., the space into which the central outlet channel 13 supplies the central stream is at the first pressure P1), and the secondary outlet channel 6 is at the second pressure P2, wherein the first pressure P1 is lower than the second pressure P2. The fluid supplied through the central outlet channel 13 typically has a higher pressure than the first pressure P1 to ensure uniform flow.

As described with reference to FIG. 2a, flow equalizing vanes 19 are located on the elongated end section 8. However, in the embodiments described here, the elongated end section 8 is absent. Therefore, a flow-leveling device 19 ′ may be provided, such as flow-leveling vanes, which are mounted on the diffuser skin 14 or the diffuser body 18 (as shown in FIG. 2b). A more detailed description is given in patent application PCT / H2008 / 050172.

Thus, a method for separating a fluid mixture using a separator for

- 6,025,118 fluid, as described above. The method may include supplying a first fluid to form a main stream, supplying a second fluid to form a central stream.

The cyclone fluid separator ΤΨ 'described with reference to FIG. 2b can be used on expansion cooling units 200.

The expander can be formed by an annular gap 3 downstream of the swirl blades 2 up to the expanding separation chamber 5 for the fluid, including the tubular neck portion 4. The separator 8EP can be formed by a separation chamber 5 for the fluid. The COM compressor may be formed by an external secondary fluid outlet 6 and a central primary fluid outlet 7.

The cyclonic separator T ^ 'for a fluid with an additional central flow described with reference to FIG. 2b is just an example, and another similar device can also be used to function as a cyclone fluid separator with an additional central stream, such as the device described in international patent application \ UO 2009/028987.

TEC turboexpander compressor.

FIG. 2c schematically depicts a TEC turbo-expander compressor that can be used on expansion cooling-based separation units 200, as one alternative to the above described T ^ 'cyclone fluid separators.

The TEC turbo-expander compressor may include a TE turbo-expander for receiving inlet 61. The TE turbo-expander can be configured with a radial or axial flow, by which the high-pressure inlet 61 expands to form an expanded flow 62. The TE turbo-expander can include a turbine rotor, which is driven by the expanding input stream 61. The generated energy can be transferred to the compressor of the vehicle to drive the compressor of the vehicle, as will be explained below.

Since energy is obtained from the expanding inlet stream 61, and the expansion is an isentropic process (i.e., a process with almost constant entropy), the expanded stream 62, which is at a lower pressure than the inlet stream 61, also has a lower temperature than the input stream 61, for example -50 ° C or lower. This causes condensation and the formation of droplets of liquid.

The expanded stream 62 is transferred to a separation tank U4, for example a reservoir U4 for low temperature separation. The droplets of liquid that have formed will be mainly removed in the bottom of the separation tank U4 and form an outlet stream 64 enriched in liquid. Other components will form a gas-rich outlet stream 63, which is discharged from the upper part of the separation tank U4.

This gas enriched outlet stream 63 is fed to a compressor TC. It will be understood that many types of compressors can be used.

The compressor TC is designed to increase the pressure of the gas-enriched outlet stream 63 with the formation of a re-compressed outlet stream 65. Again, the following relation is observed: P0 '> P2'> P1 ', where P0' represents the pressure of the inlet stream 61, P1 'represents the pressure of the expanded stream 62, and P2 'represents the pressure of the outlet stream 65, as indicated in FIG. 2s

According to the example of FIG. 2c, the TC compressor is connected to the TE expander through an 8H shaft. The shaft 8H is used to drive the compressor of the vehicle using the work received from the input stream 61 using a TE turboexpander. During application, the shaft 8H can rotate. Of course, energy transfer can be achieved in any suitable way, possibly without an 8H shaft. Power transmission can be provided by electrical means.

The TEC turbo-expander compressor shown in FIG. 2c, may be used on expansion cooling units 200.

An expander can be formed by a TE turboexpander. The separator 8EP can be formed by a separation tank U4. The COM compressor can be formed by the TC compressor. These parts are shown schematically in FIG. 2s

Joule-Thomson valve.

FIG. 26 schematically illustrates a Joule-Thomson valve that can be used on expansion cooling-based separation units 200. The skilled artisan knows many different Joule-Thomson valves. One example of a Joule-Thomson valve is shown in FIG. 26, which schematically depicts a conventional mesh valve for flow control, as supplied by Mokue16 Wack W.U., in which a fluid stream is throttled through a perforated sleeve or cage 23 that is connected to a piston-type valve body 22.

The common Mokue butterfly valve 16 shown in FIG. 26 includes a valve housing 21 in which the piston-type housing 22 is slidably mounted and connected to the perforated sleeve 23 so that when the gear 24 is rotated on the valve axis 25, the piston piston rod 26 causes the housing 22 to reciprocate

- 7,025,118 in the fluid outlet 27, as illustrated by arrow 28. The valve has a fluid outlet 29 that has an annular section 29A downstream that may span the piston 22 and / or perforated sleeve 23 and the fluid stream , which may then flow from the fluid inlet 29 to the fluid outlet 27, is controlled by the axial position of the housing 22 relative to the perforated sleeve 23 connected thereto.

A conventional sleeve 23 includes perforations 30 with grooves or holes that have a radial orientation, i.e. perpendicular to the cylindrical surface of the sleeve 23. By displacing the piston 22 in the sleeve 23 in the axial direction, the flow passage can be adjusted.

Variants of this valve are possible such that, for example, the available free pressure for isoenthalpic expansion can be used to create a swirling flow by imparting a specific geometric shape to the valve closure device and / or valve stem. Kinetic energy is then dissipated mainly as a result of quenching the vortices along the length of the pipe, extended downstream of the valve. Swirling flow can be created using perforations 30, which have a tangential component relative to the Central axis of the housing of the sleeve 23.

Downstream of the fluid outlet 27, a separator 8EP, for example, formed by a separation tank U3, such as a low temperature separator or a hydrated separator, can be placed.

Of course, other types of Joule-Thomson valves may also be used.

In general, the Joule-Thomson valve includes an EXP expander (formed by perforations 30 in FIG. 26), which may be followed by a separator 8EP (for example, formed by a separation tank U3).

Embodiments of the invention

Embodiments of the invention presented below with reference to FIG. 1, 3 and 4, show a flow chart for controlling the dew point of hydrocarbons based on expansion cooling technology, thereby using expansion separation blocks 200 based on expansion cooling, for example, using a TEC turbo-expander compressor, a Joule-Thomson valve, or a T ^ cyclone separator , T ^ ', as described above with reference to FIG. 2a-26

These embodiments describe a hydrocarbon dew point control circuit including an expansion cooling separation unit 200 and a stabilization unit 300. Upstream of the separation unit 200, a preliminary separation unit 100 may be provided, an example of which will be described first.

Embodiments use a separation unit based on expansion cooling, optionally including a re-compression unit. In some embodiments, a re-compression unit may not be present, as is the case where the process flow for controlling the dew point of hydrocarbons is based only on expansion technology using a Joule-Thompson valve. The re-compression unit can also be built in initially, for example, in the case where a cyclone separator T ^, T ^ 'is used, as described above.

Block 100 preliminary separation.

A pre-separation unit 100 may be provided, including a first separation tank U1, a heat exchanger HE1, and a second separation tank U2. The pre-separation unit 100 is designed to accept an input stream II for pre-separation, which may be an incoming gas stream including hydrocarbons. Examples of such a pre-separation unit 100 are shown schematically in FIG. 3-6 and more schematically in FIG. one.

In general, the pre-separation unit 100 may be designed to receive a gas stream, also called inlet stream II, for pre-separation, which is cooled, for example, using a first heat exchanger HE1. The first heat exchanger HE1 may be a gas-gas heat exchanger in which a relatively cold exhaust gas is used for cooling. Other cooling devices or combinations of cooling devices, for example an air cooler, a propane refrigerator, a gas-liquid heat exchanger, can also be used.

The input stream II for preliminary separation is connected to the first separation tank U1, which may be a gravitational principle separator or a separation tank of any other suitable type. The first separation tank U1 forms a first liquid-rich outlet stream L1 and a first gas-rich outlet stream C1. The first separation tank U1 is mainly used to separate free liquids.

The first gas-enriched outlet stream 01 is guided through a heat exchanger HE1 and introduced into a second separation tank U2, which may be a gravity separator or a separation tank of any other suitable type. The second separation tank Y2 forms a second liquid-rich outlet stream b2 and a second gas-enriched outlet stream 02. The second liquid-enriched outlet stream b2 may be

- 8 025118 is combined with the first liquid enriched output stream L1, inside or outside the preliminary separation units 100, and can generate an output stream for the stabilization units 300.

The second gas-rich outlet stream 02 is used as the second inlet stream 12 for the expansion-based separation unit 200.

Block 200, based on expansion cooling.

The expansion cooling separation unit 200 is adapted to receive an input stream 12 and a return feed stream P8 from stabilization units 300.

The input stream 12 can be created, for example, on the block 100 preliminary separation. In this case, the input stream 12 may be formed by the second gas-rich output stream 02.

The pressure of the inlet stream 12 may be relatively high, for example of the order of 100 bar (10 MPa), and it may have a temperature of typically 298 K (25 ° C.). The pressure is reduced by expansion in an EXP expander, such as formed by a cyclone separator T ^, T ^ 'for a fluid, as described above with reference to FIG. 2a and 2b, in a TEC turbo-expander compressor, as described above with reference to FIGS. 2c, or in the Joule-Thompson valve described above with reference to FIG. 26.

Due to the expansion, the temperature of the inlet stream 12 is significantly reduced, resulting in the formation of liquid hydrocarbons, although the outlet temperature in the case of Joule-Thomson valves may be higher than for others due to its iso-enthalpy cooling.

In the case of using a cyclone separator T ^, T ^ 'for a fluid, the resulting liquids are at least partially separated inside the cyclone separator T ^, T ^' for a fluid. The cyclone separator T ^, T ^ 'for the fluid generates a stream CE enriched in the condensed components through the external secondary outlet 6 and a gas stream 0E enriched in the gaseous components through the central primary outlet 7. The stream CE enriched in the condensed components may contain a certain amount of gas leakage, typically 30 -35%.

In the case of using a cyclone T \ U separator for the fluid according to FIG. 2a, the return feed stream P8 can be fed directly to the separation tank U3, thereby without extracting condensable components from the return feed stream P8. In the case of a cyclone separator T ^ 'for a fluid with an additional central stream, according to FIG. 2b, the return feed stream P8 is injected halfway during the expansion process, i.e. through the central outlet channel 13, and thereby the condensable components from P8 will also be obtained with an additional CE stream enriched in the condensed components. This is schematically shown in FIG. 4.

The CE stream enriched with condensable components is fed into a separation tank U3 to remove gas leakage.

The separation tank U3 may be a hydrated separator or a low temperature separator. The hydrate separator uses heat to control the formation of hydrates, while the low temperature separator requires dehydration upstream of the separation unit 200 based on expansion cooling or suppression of hydrate formation by a chemical inhibitor. The separator U3 may be a reservoir for degassing liquids, the separator U3 thereby produces an upper stream T8, mainly including a gas breakthrough, and a lower stream B8. An example of a hydrated separator is given in patent document νΟ 2006/070019.

The gas-enriched stream 0E from the cyclone separator TV, T ^ for the fluid and the upper stream T8 from the hydrate separator U3 can be combined and used to cool the inlet stream 11 for preliminary separation in the preliminary separation unit 100, after which the gas will be discharged to the outside.

In the case of using the TEC turbo-expander compressor shown in FIG. 2c, in the expansion-based separation unit 200, as an alternative to the cyclone separator TV, T ^ for fluid, the inlet stream 12 (comparable to the inlet stream 61 shown in FIG. 2c) is expanded in the TE expander to form an expanded stream E8 ( comparable to the expanded stream 62 in Fig. 2C). An example of this is shown in FIG. 5.

The expanded stream E8, which includes condensed liquids, is sent to a low-temperature separator U4. Upstream of the relatively low temperature separator U4, dehydration or inhibition of hydrate formation by chemical inhibition is required.

The low temperature separator U4 also forms an upper stream T8 (comparable to gas enriched outlet 63, in FIG. 2c) and a lower B8 stream (comparable to liquid enriched outlet 64, in FIG. 2c).

The relatively cold overhead stream T8 can be used to cool the inlet stream 11 for pre-separation in the pre-separation unit 100. After that, the upper stream T8 can be directed to the compressor of the vehicle. Compressor TC is designed to increase the pressure of the overhead stream T8 with the formation of a re-compressed output stream. Many types of compressors can be used.

Bottom stream B8 may be further processed in stabilization unit 300.

- 9 025118

In the case of using a Joule-Thomson valve, an expanded Εδ flow created downstream of the Joule-Thomson valve (comparable to valve 27 in FIG. 26), which includes condensed liquids, is sent to a separation tank U3, which, for example, may be a low-temperature separator or hydrate separator.

The expansion cooling unit 200, in accordance with which the return feed stream Ρδ from unit 300 is combined with the intermediate separation δΕΡ, is based on a cyclone fluid separator T ^ 'with a central outlet and a TEC turbine expander, i.e. before compression. Alternatively, the T \ U cyclone separator arrangement for fluid and Joule-Thomson valve is applicable. In the latter case, the return feed stream Ρδ can either be introduced into the U3 separation tank at high pressure and thereby also at a higher flow rate than in the earlier expansion-compression scheme, or a separate exhaust gas compression device must be added to combine with the first outlet stream C1 enriched in gas.

Block 300 stabilization.

Downstream of the expansion-based separation unit 200, an additional (separation) unit is provided, called a stabilization unit 300, which includes a heated separator, such as a fractionating distillation column PC. The operation of PC distillation columns and peripheral devices will be understood by a qualified professional. An example of stabilization unit 300 is shown in FIG. 3-6.

The distillation column RS may include a boiling water heater KV in the bottom part and a circuit for the reflux of phlegm KR, including an air cooler at the top.

The distillation column RS produces a fractionated bottom stream RV, which is partially re-introduced into the fractionation distillation column RS through the boiler KV. The remainder is used to preheat the inlet stream of the PC rectification column, as will be explained in more detail below.

The distillation column RS also produces a fractionated overhead stream RT, which is fed to the AC air cooler, after which it is partially re-introduced into the distillation column RS.

In the stabilization unit 300, a lower stream Βδ of separation tanks Y3, Y4 is used as the input stream, possibly in combination with the first and second liquid enriched output stream L1, L2. This is called intermediate stream 13.

Before entering the PC rectification column, the intermediate stream 13 can be fed into a static CO coagulator (known to a qualified specialist) to remove free water from the condensate. The lower stream (water) from the aircraft coagulator is led out for disposal. The CO coagulator will increase the size of droplets of free water so that it can be separated from the condensate.

When the first and second liquid enriched outflow stream b1, b2 is combined with the lower flow Βδ, the first and second liquid enriched flow outflows b1, b2 can be subjected to explosive evaporation with the formation of three phases (gas, condensate and water). The CO coagulator may not be able to process these three phases. Therefore, to solve this problem, the following additional devices can be introduced: instead of the CO coagulator, two different coagulators (not shown) can be provided, the first coagulator for the first and second output stream L1, L2, enriched with liquid, and the second coagulator for bottoms Βδ, wherein the first coagulator operates at relatively high pressure, the second coagulator operates at relatively low pressure, and the output streams from the first and second coagulators can be combined; increasing the pressure of the lower stream Βδ before combining it with the first and second output streams b1, b2, enriched with liquid, to a pressure level that is essentially equal to the pressure level of the first and second output streams b1, b2, enriched with liquid, and then removing free water in a single coagulator.

The upper stream from the coagulator TCO, i.e. cold condensate supplied is preheated in a second heat exchanger HE2, i.e. liquid-liquid heat exchanger, using relatively hot stabilized condensate, which is present in the fractionated bottom stream RV. After the second heat exchanger HE2, the upper stream from the CO coagulator is directed as an input stream to the fractionation distillation column PC.

The use of a PC distillation column makes it possible to keep the gas and condensate obtained by explosive evaporation at a higher pressure than atmospheric, since the distillation column can operate at a pressure between 15-30 bar (1.5-3.0 MPa).

As mentioned, the fractionated overhead stream RT, which includes relatively light gaseous hydrocarbons, is partially re-introduced into the distillation column PC. However, another part, for example, obtained from the AC air cooler, is reintroduced into the separation unit 200, based on expansion cooling, using a jet pump 1Ρ.

Jet pump 1Ρ.

According to embodiments, a 1Ρ jet pump is provided which is intended to accept a portion of the fractionated overhead stream PT as an input stream, also called intermediate return feed stream 14. Examples of the 1Ρ jet pump are shown in FIG. 1 and 3 - 10 025118

6. The intermediate return feed stream 14 includes relatively light gaseous hydrocarbons and typically has a pressure of 15-30 bar (1.5-3.0 MPa).

The intermediate return feed stream 14 is then sent to the 1P jet pump. Jet pumps are known to the skilled person and are also often referred to as an injector or ejector.

The pressure of the intermediate return feed stream 14 is increased using a high pressure of the feed stream 12. The pressure of the intermediate return feed stream 14 is typically 15-30 bar (1.5-3.0 MPa), the pressure of the input stream 12 is typically 100 bar (10 MPa) . By mixing them using a jet pump 1P, a return feed stream P8 can be created with a pressure of, for example, 50 bar (5.0 MPa) or the like. Thus, the pressure of the return feed stream P8 is a higher pressure than the pressure at which the fractionation distillation column PC operates, although lower than the pressure of the feed stream 12. The pressure of the intermediate return feed stream 14 can thereby be increased to be higher than the pressure before re-compression of the main process stream in the COM compressor, or higher than the pressure in the separation tanks U3, U4.

In the case of using a cyclone separator T ^ 'for a fluid with an additional central stream, the pressure of the return feed stream P8 may be higher than the pressure P1 representing the pressure in the position of the central outlet channel 13. In the case of using a turbine expander TEC, the pressure of the return feed stream P8 may be higher pressure of the low temperature separator U4, and in the case of using a cyclone separator T \ U for the fluid according to FIG. 2a or application of the Joule-Thomson valve of FIG. 26, the pressure of the return feed stream P8 may be higher than the pressure of the separation tank U3 (for example, whether it is a low temperature separator or a hydrated separator).

The return feed stream P8 is then reintroduced into the expansion cooling separation unit 200. The position in which the return feed stream P8 is reintroduced may vary for various embodiments. It may be downstream or halfway relative to the expander and upstream relative to the COM compressor, if the COM compressor is present.

Optionally, the introduction position of the return feed stream may be upstream of the expander, as will be explained in more detail below. If the position for introducing the return flow is upstream relative to the expander, an additional device for compressing the exhaust gas (not shown) is necessary in order to raise the pressure of the return flow P8 to the level of P0. However, this additional device for compressing the exhaust gas may be relatively small, since the pressure is already elevated to some extent using the 1P jet pump.

Alternatively, the return feed stream P8 may be fed back to the separation tank U3, without any additional gas compression device being required.

FIG. 1 shows a more schematic flow chart, which is based on the embodiments described with reference to FIG. 1, 3-6.

Thus, according to one embodiment, a gas conditioning system is provided including an expansion cooling separation unit 200 and a stabilization unit 300, the separation unit 200 including an EXP expander and a separator 8EP, and is adapted to receive an input stream 12, unit 300 stabilization includes a distillation column PC and is designed to receive the intermediate stream 13 from the block 200 separation, and the system further includes a jet pump 1P. designed to receive at least part of the fractionated overhead stream PT and part of the input stream 12 ', taken upstream relative to the expander expander, to combine them into the return feed stream P8, which is reintroduced into the separation unit 200 in the insertion position of the return feed stream.

As described, expansion cooling-based separation unit 200 is designed to receive the gaseous fluid inlet stream 12, expand and thereby adiabatically cool the inlet stream 12 in the EXP expander, so that at least some of the initially gaseous components become supersaturated and condensed with the creation of droplets of liquid in a gaseous fluid, taking at least part of the expanded flow in the separator 8EP, containing at least a separation tank U3, U4, pre designated to receive the overhead stream and a bottoms stream T8 B8 and optionally recompressing at least a portion of the received input stream 12 in the compressor COM. The intermediate stream 13 from the separation unit 200 is a lower stream B8.

According to one embodiment, the stabilization unit 300 may additionally include a CO coagulator and a second HE2 heat exchanger, while the CO coagulator is designed to receive an intermediate stream 13, the CO coagulator produces an upper TCO stream, which is heated by a second HE2 heat exchanger before being sent to the PC distillation column. The TCO top stream may also be called the dehydrated TCO top stream condensate.

- 11 025118

The distillation column PC is designed to separate at least a portion of the intermediate stream 13 and form a fractionated upper stream RT and a fractionated lower stream RV.

The pressure of the return feed stream P8 is at a level between the pressure of the fractionated overhead stream PT and the inlet stream 12 and is equal to or higher than the pressure in the insertion position of the return feed stream. In some cases, an additional compressor may be required. However, such a compressor may be smaller due to the increase in pressure generated by the 1P jet pump.

As described, according to one embodiment, the expansion-based separation unit 200 includes a TTO, TTO 'cyclone separator for fluid or a Joule-Thomson valve and a separation tank U3 in which an expander and an 8EP separator are implemented. The separation tank U3 may be a low-temperature separator L8 or a hydrated separator.

The system may further include a pre-separation unit 100 including at least one separation tank U1, U2 and a first heat exchanger HE1, and designed to receive the incoming gas stream II, which is cooled in the first heat exchanger HE1, and to separate the incoming gas stream using at least one separation tank U1, U2 to form a gas-rich outlet stream 02 and a liquid-enriched outlet stream L1, L2, the gas-enriched outlet stream 02 forms an input stream 12. The preliminary separation unit 100 is actually also a separation unit, but is mainly used for preparing fluids for the separation unit 200 based on expansion cooling.

In addition, a gas conditioning method is provided, according to which an input stream 12 is supplied to the separation unit 200 based on expansion cooling and an intermediate stream 13 is formed therein;

serves the intermediate stream 13 in the distillation column PC block 300 stabilization; create in the distillation column PC fractionated upper stream RT and fractionated lower stream RV;

at least a portion of the fractionated overhead stream RT and a portion of the inlet stream 12 ′, selected upstream of the expander expander, are fed to the jet pump 1P to combine them into the return feed stream P8;

reintroducing the return feed stream P8 to the expansion cooling-based separation unit 200 in the introduction position of the return feed stream.

Upstream of the expander expander.

According to one embodiment, the return feed stream P8 is re-introduced upstream of the expander, i.e. upstream of the TTO cyclone separator for the fluid, the TTO 'cyclone separator for the fluid with an additional central stream, a TEC turboexpander-compressor, or a Joule-Thomson valve, where it could be combined with inlet stream 12. Alternatively, the return feed stream P8 may be reintroduced into the pre-separation unit 100, for example, into the first gas-rich outlet stream 01.

However, it will be understood that since the pressure of the return feed stream P8 is lower than the pressure of the feed stream 12, additional measures, such as an additional compressor, are required to increase the pressure of the return feed stream P8.

Therefore, according to one embodiment, the process flow diagram further includes a compressor for increasing the pressure of the return feed stream P8, and the position for introducing the return feed stream is upstream of the expander. In this case, a relatively small additional exhaust gas compressor unit may be necessary to increase the pressure of the return feed stream P8 to a level at least approximately corresponding to pressure P0, which is the pressure upstream relative to the separation-based separation unit 200, which is based on expansion cooling, which typically can be of the order of 100 bar (10 MPa). Since the pressure of the return feed stream P8 is relatively high as a result of the action of the 1P jet pump, a relatively small and economical compressor is needed.

Halfway to the expander expander.

According to one embodiment, the return feed stream P8 is reintroduced during expansion in the expander expander, wherein the insertion position of the return feed stream is halfway to the expander. The return feed stream P8, for example, is reintroduced using a central outlet 13, as discussed above with reference to FIG. 2b. The central outlet channel 13 is positioned on the downstream side with respect to the central body 10 and is directed toward the neck portion 4. The position and direction of the central outlet channel 13 substantially coincide with the central axis I. The central outlet channel 13 is for introducing a central stream into the TTO cyclone separator 'for fluid.

- 12 025118

The cyclone separator T ^ 'for the fluid with an additional central stream has a Central outlet channel 13, which can be used to introduce obtained by explosive evaporation of gas as a Central stream. The required inlet pressure is significantly lower than the inlet pressure required for the primary inlet gas, i.e. the pressure is upstream relative to the pear-shaped central body 10. The secondary inlet gas is mixed into the primary stream after expansion and re-compression, after which it is used for pre-cooling the feed gas.

The fluid introduced through the central outlet channel 13 may be a fluid with a pressure higher than pressure P1 (discussed above with reference to FIG. 2b), but with a pressure lower than pressure P0.

Although not shown in the drawings, a cyclonic fluid separator T ^ 'with an additional central stream may be provided with a channel 12 to create a central outlet channel 13 with a fluid stream. According to one example, one or more rungs 21 can be hollow and connected to the duct 12 as guides for flowing to the central outlet channel 13.

Downstream of the expander expander.

According to one embodiment, the return feed stream Ρδ is re-introduced downstream of the expander.

For example, in the case where the expansion-based separation separation unit 200 includes a TE turbo-expander using an EXP expander, a separation tank U4 using a separator δΕΡ, and a compressor TC using a COM compressor, a position for introducing a return feed stream may be provided as in the inlet to the separation tank U4, for example, as the reservoir U4 for low temperature separation described above with reference to FIG. 2s

According to one alternative embodiment, the return feed stream Ρδ, for example, is reintroduced into the introduction position of the return feed stream, which is upstream of the TC compressor, but downstream of the low temperature separation tank U4.

This can be done when the return feed stream Ρδ is unsaturated vapor. If the return feed stream Ρδ is saturated steam, liquids may form when expansion to pressure P1 ′ occurs, and therefore the return feed stream Ρδ can be reintroduced into tank U4.

Thus, for the TEC turboexpander-compressor, the forced gas is combined with the main process stream in the U4 low temperature separator or at the inlet of the ТС turbocompressor, after which the common stream is used to pre-cool the first gas-enriched outlet stream C1, after which it is re-compressed using the ТС compressor, driven by a TE turboexpander, and subsequently brought out.

In the case of using a cyclone separator T ^, T ^ 'for a fluid without an additional central flow or with such a return feed stream Ρδ can be reintroduced after compression, i.e. into the hydrated separator U3. Thus, the position of the introduction of the return feed stream can be on the separation tank U3, U4.

In addition, it should be noted that in the embodiments described above with reference to FIG. 4 and 5 (i.e., a cyclone separator T ^ 'for a fluid with an additional central stream and a TEC turboexpander compressor), a return feed stream Ρδ is mixed with an isentropic-expanded stream in a cyclone separator T ^' for a fluid, or with an isentropic-expanded stream in separation tank U4 turbine expander-compressor TEC. Thus, the feed return stream Ρδ is dew point-adjusted cold gas / liquid in front of the compression unit. Moreover, in the embodiments described with reference to FIG. 3 and 6 (i.e., with a T \ U cyclone separator for the fluid and a Joule-Thomson valve), the return feed stream Ρδ is mixed with the isoanthalium-expanded stream in tank U3. Therefore, for these last two versions, a stronger motive stream 12 'is needed in order to obtain a higher pressure to match the higher Y3 pressure, thereby increasing the flow of the (untreated) return feed stream Ρδ and thereby polluting the outward gas. Alternatively, an additional compressor unit is needed to introduce a feed Ρδ of 12.

Benefits.

The above embodiments of the invention provide a number of advantages in comparison with the known schemes for controlling the dew point of hydrocarbons and conditioning, for example, with condensate stabilization by explosive evaporation of the condensate when pressure drops to atmospheric pressure.

The above embodiments are relatively simple process flow diagrams in which the gas is conditioned and the condensates are stabilized without being flared. Since flaring is not required, a significant reduction in emissions of CO ₂ and the like can be achieved, which is preferable from an environmental point of view.

Embodiments including a cyclone separator T ^, T ^ 'for a fluid or

- 13 025118 TEC turboexpander-expander, or Joule-Thomson valve, also have the advantage that small additional compressor units for the off-gas are not required or are required, since the off-gas does not need to compress the off-gas. As a result, energy consumption is also reduced, and therefore, CO ₂ emissions and the like are reduced.

In general, the complexity of the technology is reduced because no exhaust gas compressors are installed. This leads to a reduction in investment since the use of the ΙΡ jet pump is a relatively simple technology. In addition, operating costs are reduced since no exhaust gas compressor is required.

Variants of execution make it possible to stabilize and store condensate in remote places where there is no piping system for removing condensate or oil and where transportation of (Destabilized) condensate is not preferred.

In addition, equipment with rotating parts is not used in the technological scheme, which includes the cyclone separator Т ^, Т ^ 'for the fluid, which reduces maintenance and thus operating costs and increases the period of operation, in comparison with the scheme based on the turboexpander compressor TEC.

The cyclone separator T ^, T ^ 'for the fluid is able to condition the gas in a single installation, thereby regulating the dew point of water in combination with regulating the dew point of hydrocarbons. No additional dehydration or chemical inhibition is required, which are necessary in the technological scheme based on the TEC turboexpander-compressor.

Additional notes.

The above descriptions are for illustration, but not limitation. Thus, it will be understood by a person skilled in the art that modifications of the invention may be made within the scope of the appended claims.

Claims (11)

CLAIM 1. A system for conditioning the gas, comprising a separator of the initial inlet gas stream into two parts; an expander for receiving the first part of the input stream, in which the expansion and adiabatic cooling of the input stream is carried out; a separator having an inlet connected to the outlet of the expander, an outlet for a liquid intermediate stream and a gas outlet; distillation column connected to the output of the separator for the liquid intermediate stream and configured to create a fractionated upper stream and fractionated lower stream; a jet pump, one input of which is connected to the top stream of the distillation column, and the second is designed to accept the second part of the initial input stream, the output of the jet pump being connected to a separator or to an expander to direct the resulting return feed stream into it. 2. The system according to claim 1, in which the separator contains at least one separation tank designed to form an upper stream and a lower stream. 3. The system according to any one of paragraphs. 1 or 2, which further comprises a coagulator and a heat exchanger, while the coagulator is designed to receive an intermediate stream from the separator and create an upper stream, and the heat exchanger is designed to heat the specified upper stream before being sent to the distillation column. 4. The system according to any one of claims 1 to 3, which contains a cyclone fluid separator or a Joule-Thomson valve as an expander and a separation tank as a separator. 5. The system according to claim 4, in which the position of the means of maintaining the return feed stream is in the middle of the expander. 6. The system according to claim 5, which contains a cyclone separator for the fluid and a compressor having a casing in which the Central housing is placed with the formation of an annular gap between the inner surface of the casing and the outer surface of the Central housing and creating a tapering inlet section for the fluid, and the cyclone a fluid separator is designed to facilitate the passage of the main stream through the tapering inlet section, and the Central housing contains a Central outlet channel for introduction ENTRAL flow into the main flow, whereby the central position of the discharge channel forms a return feed stream introduction. 7. The system according to claim 4, in which the position of the introduction of the return feed stream is located on the separation tank. 8. The system according to any one of claims 1 to 4, which contains a turboexpander as an expander, and a separation tank and compressor as a separator. 9. The system of claim 8, in which the position of the introduction of the return feed stream is located on the inlet channel into the separation tank. 10. The system according to any one of claims 1 to 9, further comprising a pre-separation unit comprising at least one separation tank and a heat exchanger, and is configured to receive an inlet gas stream cooled in the heat exchanger and separate the inlet gas stream by at least one separation tank with the formation of a gas-rich outlet stream and a liquid-enriched outlet stream, the gas-enriched outlet stream being the input stream to the expander. 11. The method of conditioning the gas using the system according to any one of claims 1 to 10, according to which the input stream is divided into two parts; supplying one part of the input stream to the expander, in which a stream is formed which directs the separator to obtain an intermediate stream; supplying an intermediate stream to a distillation column from a separator; create a fractionated upper stream and a fractionated lower stream in a distillation column; supplying at least a portion of the fractionated overhead stream and a second portion of the inlet stream, taken downstream to the expander, to a jet pump to combine the two streams into a return feed stream; the return feed stream from the jet pump is introduced either into the expander or into the separator.