KR100939053B1 - Integrated ngl recovery and liquefied natural gas production - Google Patents

Abstract

Separation of methane from the mixture 110 of ethane and heavy hydrocarbons, in particular natural gas, using a scrub column 114 may result in additional reflux 136 obtained in the ethane rich stream 130 from the fractionation 128 of the bottom liquid. In this separation, the mixture separates into a methane rich upper layer 116 which partially condenses at 122 to provide reflux to column 114, and a lower liquid 126 minus liquid methane. Preferably, absorbent liquid 140 from fractionation 128 is also introduced into the scrub column. Steam portion 120 remaining after partial condensation may be liquefied at 122 to provide LNG product 124.

Description

INTEGRATED NGL RECOVERY AND LIQUEFIED NATURAL GAS PRODUCTION}

The present invention relates to the separation of methane from a mixture of ethane and heavy hydrocarbons, including but not limited to the integration of natural gas liquid (NGL) from natural gas (NG) and the generation of liquefied natural gas (LNG). Has application for the process.

Natural gas mainly contains small amounts of components, including methane, and heavy hydrocarbons. Liquefied natural gas consists mostly of methane. Hydrocarbons heavier than methane are generally condensed and recovered as natural gas liquids and fractionated to yield useful hydrocarbon products.

A typical NG liquefaction system includes a scrub column fed with natural gas or pipeline gas as raw material and producing NGL as methane rich upper vapor and bottom liquid. Some of the methane rich upper vapor is partially condensed to provide reflux for the column and the other is liquefied to provide the LNG product. The bottom liquid is fractionated to obtain individual hydrocarbons and / or hydrocarbon cuts (classification) as useful products.

The efficiency of liquefaction improves with increasing pressure, so the NG liquefaction pressure must be significantly higher than the critical pressure of methane to minimize the power consumption of the LNG process. However, recovery of heavy hydrocarbons by the scrub column becomes difficult as the pressure increases, and it is not possible to separate the mixture at pressures above the critical pressure. Therefore, the scrub column must be operated at a pressure significantly lower than the critical pressure of methane in order to satisfactorily separate. A common solution is to expand the natural gas feed to the scrub column and then compress the upper vapor. Work obtained from isentropic expansion of natural gas feed may be used to drive the upper compressor (s) at least partially. This solution is disclosed in US-A-4065278, published December 27, 1977.

By recycling the heavy components obtained from the NGL fraction as the absorbent liquid on or near the top of the scrub column, it is possible to avoid expansion of the natural gas feed to the scrub column prior to compression of the upper vapor. For example, Chen-Hwa Chiu (Oil and Gas Journal, Nov. 24, 1997, pp. 56-63) uses heavy alkanes recirculation, such as all or part of the C ₄ NGL classification, for scrub columns in LNG processes. It has been reported that the critical pressure of the separated mixture can be raised thereby increasing the operating pressure on the scrub column. In an exemplary process, some or all of the C ₄ NGL fraction recovered from the debutane group is recycled.

WO 01101307 / US-A-2003005722 / US-B-6,742,358 (published December 2, 2002, January 9, 2003, June 1, 2004, respectively) indicates that the top reflux for the scrub column Disclosed is an LNG process provided by condensing steam withdrawn from an intermediate position. This document also discloses a process in which the vapor part and the liquid part of the partially condensed feed gas are separately classified and the bottom liquid fractionated from the vapor part provides an intermediate reflux or top reflux for the fractionation of the liquid part. In both of these processes, the upper vapor from the scrub column is compressed prior to liquefaction.

DE-A-10205366 (published Aug. 21, 2003) discloses an LNG process in which ethane enriched ethane from a scrub column is cooled and delivered to a second column to remove heavier excess hydrocarbons. have. The bottom liquid of the second column provides reflux for the scrub column. Preferably, the C ₄ / C ₅ NGL classification provides reflux for the second column. The rectification and absorption functions of the two columns can be integrated into a single column.

US-A-6662589 / EP-A-1469266 (published 16 December 2003 and 20 October 2004, respectively) is a natural gas feedstock and methane rich reflux as an NGL classification absorbent liquid consisting of components heavier than ethane. An LNG process is disclosed that is supplied to a scrub column at locations between streams. In an exemplary embodiment, the reflux stream is obtained by partially condensing the upper vapor from the scrub column. The scrub column top layer is not compressed prior to liquefaction to provide LNG product.

WO 2004/010064 (published January 29, 2004) discloses an LNG process in which a C ₄ / C ₅ NGL fraction is fed directly or indirectly to a scrub column to provide further reflux. The fraction is fed to the column at or above a reflux feed prepared by partially condensing the column overhead vapor.

The critical pressure of the mixture in the scrub column can also be raised by refluxing the column using an ethane rich stream. It also allows for good separation of C ₂ and C ₃ and recovery of propane (C ₃ ) from NGL.

WO-A-0188447 / US-A-6,401,486 (published on November 22, 2001, June 11, 2002, respectively) discloses that a scrub column contains a very small amount of propane and is mostly condensed by steam consisting of methane and ethane. An LNG process is disclosed that provides a top reflux for a gas. The scrub column overhead vapor is fully liquefied to provide the LNG product, and the scrub column bottom is fractionated in the NGL purification column. The vapor that condenses to provide the top reflux

(i) upper vapor from the NGL fraction and optionally flashed vapor obtained by flashing the liquefied, preferably supercooled scrum column upper layer to near atmospheric pressure,

(ii) the wake of the feed gas portion,

(iii) flashed vapor obtained by flashing a liquefied, preferably supercooled, scrub column top to near atmospheric pressure, or

(iv) a portion of the upper layer of the liquefied and preferably subcooled scrub column

Can be obtained from In options (i), (iii) and (iv) above, additional reflux to the scrub column may be provided by condensing the wake of the feed gas portion, but both NGL fractionation and the partially condensed scrub column top layer. There is no teaching in providing reflux from In these processes, the scrub column top layer need not be compressed prior to liquefaction.

EP-A-0178207 / US-A-4,690,702, published April 15, 1986 and September 1, 1987, respectively; DE-A-3802553 / US-A-4,952,305, published August 3, 1989 and August 28, 1990, respectively; And EP-A-0535752 / US-A-5,291,736 (published on April 7, 1993 and March 8, 1994, respectively) are all generated by the reflux of a scrub column by condensing the upper vapor obtained from the NGL fraction. An LNG process is disclosed that is provided by a mixture of methane and ethane. None of these patents disclose obtaining reflux by partially condensing the upper product.

Recovery of NGL and natural gas products combines the benefits of reflux obtained by partially condensing the scrub column top layer with the benefits of ethane rich reflux and absorbent liquid in an efficient manner, thereby providing thermodynamic efficiency, equipment simplification, and propane and butane It has been found that it can be improved in terms of recovery of useful components such as

In the broadest aspect, the present invention provides a process for recovering heavier components than methane from a mixture of methane mixed with ethane and heavy hydrocarbon (s), the process comprising

Introducing a natural gas source into the scrub column at a first location;

Extracting from the scrub column a first upper vapor stream subtracting a component heavier than methane and a bottoms stream enriched in components heavier than methane;

Cooling and partially condensing the first upper vapor stream to form a first biphasic stream;

Separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating the bottoms stream into an ethane rich stream and one or more streams enriched in components heavier than ethane; And

Introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a location selected from a second location and a third location above the first location.

In a preferred embodiment of the present invention, the ethane rich stream obtained from the NGL fraction, preferably the upper layer of deethane group, is condensed, pumped, mixed with the reflux stream obtained by partially condensing the scrub column upper vapor, scrub column, Preferably it is recycled to the scrub column reflux drum. This allows the scrub column to operate at higher pressures by increasing the critical pressure of the mixture and also improves the separation of ethane and propane. The ethane rich stream can be fully condensed using mixed coolant (MR) cooling available in the main heat exchanger of the LNG process to maximize the benefit.

It may also be useful to use heavy recycle streams, specifically pentane and isopentane. The heavy recycle stream may be introduced into the reflux drum or directly into the scrub column. The heavy recycle stream and the light recycle stream may be mixed and may be cooled separately, or may preferably be mixed with the reflux stream obtained by condensing the scrub column overhead vapor. The reflux obtained by condensing the supernatant vapor generally exceeds about 80% of the total liquid reflux (including any heavy recycle stream) to the scrub column. In a preferred embodiment, cooling takes place in the warmed bundle of the main LNG process heat exchanger.

As noted above, the present invention provides a process for recovering heavier components than methane from a mixture of methane mixed with ethane and heavy hydrocarbon (s) in the broadest aspect of the process.

Introducing a natural gas source into the scrub column at a first location;

Extracting from the scrub column a first upper vapor stream subtracting a component heavier than methane and a bottoms stream enriched in components heavier than methane;

Cooling and partially condensing the first upper vapor stream to form a first biphasic stream;

Separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating the bottoms stream into an ethane rich stream and one or more streams enriched in components heavier than ethane; And

Introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a location selected from a second location and a third location above the first location.

In an aspect of the corresponding apparatus, the present invention provides an apparatus for recovering a heavier component than methane from a mixture of methane mixed with ethane and heavy hydrocarbon (s) by the process of the aforementioned aspect, wherein the apparatus is

Scrub column;

Conduit means for introducing a natural gas feed into the scrub column at a first location;

Conduit means for withdrawing a scrub column from the first upper vapor stream subtracting the component heavier than methane and the bottoms stream enriched in the component heavier than methane;

Heat exchange means for cooling and partially condensing the first upper vapor stream to form a first two-phase stream;

Separating means for separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Conduit means for introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating means for separating the bottoms stream into an ethane rich stream and one or more streams enriched in components heavier than ethane; And

A conduit means for introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a position selected from a second position and a third position above the first position.

In an embodiment of the preferred process, the present invention provides a process for obtaining liquefied methane from a mixture of methane mixed with ethane and heavy hydrocarbon (s), the process comprising:

Introducing a natural gas source into the scrub column at a first location;

Extracting from the scrub column a first upper vapor stream subtracting a component heavier than methane and a bottoms stream enriched in components heavier than methane;

Cooling and partially condensing the first upper vapor stream to form a first biphasic stream;

Separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Liquefying a second upper vapor stream;

Introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating the bottoms stream into an ethane rich stream and one or more streams enriched in components heavier than ethane; And

Introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a location selected from a second location and a third location above the first location.

In a preferred embodiment of the device, the present invention provides a device for obtaining liquefied methane from a mixture of methane mixed with ethane and heavy hydrocarbon (s) by a process according to aspects of the preferred process described above,

Scrub column;

Conduit means for introducing a natural gas source into the scrub column at a first location;

Conduit means for withdrawing a scrub column from the first upper vapor stream subtracting the component heavier than methane and the bottoms stream enriched in the component heavier than methane;

Heat exchange means for cooling and partially condensing the first upper vapor stream to form a first two-phase stream;

Separating means for separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Heat exchange means for liquefying the second upper vapor stream;

Conduit means for introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating means for separating the bottoms stream into an ethane rich stream and one or more streams enriched in components heavier than ethane; And

A conduit means for introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a position selected from a second position and a third position above the first position.

As mentioned above, the feed is preferably a cooled natural gas feed and the second upper vapor is liquefied to provide a liquefied natural gas product.

The ethane-rich second reflux stream can be fed to the scrub column separately from the methane-rich first reflux stream, but it is preferred that the methane is mixed with the first rich reflux stream prior to being introduced into the scrub column. . The ethane rich stream may be partially or fully condensed before the methane is mixed with the rich first reflux stream. Proper mixing takes place either upstream of the reflux drum or at the reflux drum, or by feeding the first two-phase stream to the bottom of the absorption column to which the ethane-rich second reflux stream is fed as reflux.

The ethane rich stream, either alone or preferably mixed with one or more other process streams, is then condensed at a temperature below the temperature of the natural gas feed to the scrub column, the condensed stream as a second ethane rich reflux stream. Pumped before being introduced into the scrub column. The temperature is generally below -32 ° F (-35.5 ° C).

Generally, the ethane rich stream 130 is the upper vapor of the deethane group. Since methane can be removed from the ethane rich stream, the second reflux stream is ethane essential. Preferably, the second reflux stream comprises less than about 0.05% propane.

In general, the first reflux stream enriched in methane makes up at least about 80% of the total reflux (ie, the liquid fed to the scrub column over the first location) and the second reflux stream is less than about 20% of the total reflux. to be.

Propane and / or butane contained in the natural gas feed, preferably greater than 90% and more preferably greater than 96%, is recovered from the bottom stream as a product.

As shown in FIG. 6, the first upper stream can be partially condensed in two stages, with the liquid portion obtained from each condensation being fed to the scrub column as reflux.

In a preferred embodiment, the process of the present invention,

Introducing a natural gas source into the scrub column at a first location;

Extracting from the scrub column a first upper vapor stream subtracting a component heavier than methane and a bottoms stream enriched in components heavier than methane;

Cooling and partially condensing the first upper vapor stream to form a first biphasic stream;

Separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating the bottoms stream into at least two streams enriched in ethane-rich components, including an ethane rich stream and an absorbent liquid stream enriched in component (s) heavier than ethane;

Introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a location selected from a second location and a third location above the first location; And

Introducing an absorbent liquid into the scrub column at a position selected from a second position, a third position, and a fourth position above the first position.

In an embodiment of the corresponding preferred device, the device of the present invention,

Scrub column;

Conduit means for introducing a natural gas source into the scrub column at a first location;

Conduit means for withdrawing a scrub column from the first upper vapor stream subtracting the component heavier than methane and the bottoms stream enriched in the component heavier than methane;

Heat exchange means for cooling and partially condensing the first upper vapor stream to form a first two-phase stream;

Separating means for separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane;

Conduit means for introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location;

Separating means for separating the bottoms stream into at least two streams enriched in components heavier than ethane, including an ethane rich stream and an absorbent liquid stream enriched in component (s) heavier than ethane;

Conduit means for introducing a second reflux stream enriched in ethane from the ethane rich stream into a scrub column at a position selected from a second position and a third position above the first position; And

Conduit means for introducing the absorbing liquid into the scrub column at a position selected from a second position, a third position, and a fourth position above the first position.

All of the features described above in connection with the broadest aspects apply to this preferred embodiment.

The absorption liquid may comprise C ₄ hydrocarbon (s), but preferably C ₅₊ hydrocarbon (s).

The absorbent liquid may be fed to the scrub column separately from either a second reflux stream enriched in ethane or a first reflux stream enriched in methane. However, the absorbent liquid is preferably mixed with at least one of the methane-rich first reflux stream and the ethane-rich second reflux stream 136 prior to introduction into the scrub column. For example, the absorbent liquid may be mixed with at least one of the first two-phase stream and the ethane-rich second reflux stream upstream of the reflux drum or in the reflux drum, or the second liquid rich in the absorbent liquid and optionally ethane. The first two-phase stream may be fed to the bottom of the absorption column where the reflux stream is fed as reflux. The absorbing liquid may be mixed with the first upper vapor stream prior to partially condensing the first upper vapor stream to form a first biphasic stream and / or condensing the gaseous ethane rich stream to form a second reflux stream. It can be mixed with a gaseous ethane rich stream prior to providing.

The mixed absorption liquid and gaseous ethane rich stream can be phase separated and the liquid portion fed to the scrub column above the first location. The liquid portion may be mixed with the first upper stream prior to partially condensing the first upper stream to provide a first biphasic stream. The steam portion can be condensed, and the condensed stream is fed to the scrub column above the first location and added to the second upper steam prior to liquefaction, or partially condensing the upper steam to provide a first two-phase stream. Prior to mixing with the first upper stream. Both the condensed vapor portion and the liquid portion may be mixed with the first upper stream prior to partially condensing the first upper stream to provide a first two-phase stream.

Generally, the absorbing liquid comprises less than about 10% of the total reflux (ie, the liquid supplied to the scrub column above the first location).

Hereinafter, with reference to the accompanying drawings of the presently preferred embodiments of the invention will be described by way of example only.

1 illustrates one embodiment of the present invention.

FIG. 2 illustrates a variation of the embodiment of FIG. 1, where reflux drum 118 is replaced with absorption column 218.

FIG. 3 illustrates another variation of the embodiment of FIG. 1, in which the ethane rich stream 130 and the “absorbent liquid” stream 140 are combined to form a single stream 330.

FIG. 4 illustrates a variation of the embodiment of FIG. 3, in which the mixed second reflux and absorbing liquid stream 330 are phase separated at 430 .

5 is a variation of the embodiment of FIG. 4, in which the separated vapor portion 436 is compressed, cooled and condensed, and the resulting stream 536 is mixed with the liquid portion 438.

FIG. 6 is another of the embodiment of FIG. 4 in which the upper vapor 116 from the scrub column 114 condenses in two stages 612 and 122 to provide separate reflux streams 619 and 626 to the scrub column. The variant is shown.

Referring to FIG. 1, pretreated compressed natural gas feed 110 comprising predominantly methane together with heavy hydrocarbons in the C ₂ -C ₆ range containing trace amounts of water, acidic gases such as CO ₂ and H ₂ S, And other impurities, such as mercury, are cooled in the heat exchanger 112 in the range of about -20 ° F. (-29 ° C.) to about −40 ° F. (-40 ° C.) and fed to the scrub column 114. In general, the pressure of the natural gas raw material 110 ranges from about 600 to about 900 psia (4 to 6.25 MPa), and the temperature of the natural gas raw material is approximately similar to ambient temperature. Heat exchanger 112 performs multistage cooling by vaporizing propane at different pressures. Any other cooling means can be used, such as vaporizing the mixed coolant in a single heat exchanger. The steam portion of stream 110, or stream 110 downstream of heat exchanger 112, may be throttled or expanded into column 114 with isentropy. The energy obtained from the expansion can be used to at least partially compress other vapor streams, such as process streams 116, 120, 150 or 156.

The scrub column 114 separates the natural gas feed into bottom liquids 126 and 127 enriched with heavy hydrocarbons and a "first" upper vapor stream 116 enriched in methane. A portion of the bottom liquid 127 is vaporized in the reboiler 128 to provide boiling to the column 114. Reboiler 128 may provide a heat duty using a portion of feed stream 110 or any other suitable process stream. The column may also have an intermediate reboiler and the feed stream portion may also provide heat load for the intermediate reboiler. The remaining bottom liquid 126, commonly referred to as natural gas liquid (NGL), is fed to the NGL fractionation system 128. In NGL fractionation systems, NGL is generally depressurized and separated using known separation devices such as deethane groups, depropane groups, and / or debutane groups to provide fractionation of two or more hydrocarbons. The bottom liquid 126 contains a stream (ethane rich stream) containing very small amounts of propane and containing methane and ethane, and mainly C ₃ , C ₄ , and C ₅₊ hydrocarbons (ie n-pentane, isopentane, and Heavier hydrocarbons). The ethane rich stream 130 is generally on top of the deethane group and contains less than about 0.05% propane.

The use of a second reflux stream 136 enriched in ethane results in a high recovery of propane (96-99%) and a high recovery of butane (almost 100%) in the fractionation system.

Some of the C ₅₊ hydrocarbons are _withdrawn as “absorber” liquid 140, up to scrub column pressure (ie, sufficient pressure to introduce the hydrocarbons into scrub column 114, including pressure drop and static pressure of the apparatus). Pumped by pump 142, cooled against vaporizing propane in heat exchanger 144, further cooled in main heat exchanger 122, and introduced into reflux drum 118, obtained from NGL fractionation. It is introduced in admixture with two reflux streams or directly as shown in phantom. Heat exchanger 144 may be located before or after pump 142.

In a preferred embodiment, the absorbing liquid 140 is mixed with the second reflux stream 136 prior to introduction into the reflux drum 118 because it allows equilibrium and some absorption to occur in the conduit.

As shown in phantom, the absorbing liquid 140 can be supplied directly to or near the top of the scrub column 114, or in a preferred embodiment a first upper vapor stream upstream of the main heat exchanger 122 ( 116).

The ethane rich stream 130 is cooled and partially condensed to the propane vaporizing in the heat exchanger 132, cooled in the main heat exchanger 122 to fully condense, and pumped to the scrub column pressure by the pump 134. Preferably mixed with absorbent liquid 140 and introduced into the reflux drum as stream 136. Any non-condensable vapor upstream of the pump 134 may be separated and condensed in the central bundle of the main heat exchanger 122 and mixed with the liquefied natural gas product 124.

Absorbent liquid 140 may also be obtained purely or mixed from light products of NGL classification, such as C ₃ and C ₄ hydrocarbons. The absorbent liquid may consist essentially of C ₅ hydrocarbons and does not include C ₆ and heavier components that may be excluded from further distillation columns.

Stream 130 may be nearly pure ethane and methane is excluded from further distillation column. Some of the ethane or a mixture of ethane and methane can be recovered as a product.

The first upper vapor stream 116 is cooled in the warmed bundle of the main heat exchanger 122 to partially condense and is introduced into the reflux drum 118. The first upper vapor stream may be compressed (not shown) prior to cooling in the main heat exchanger 122. The liquid portion is returned to the scrub column as "first" liquid reflux 119. The methane-rich “second” vapor portion 120 is liquefied in a cold bundle at the center of the main heat exchanger and preferably supercooled to provide the LNG product 124.

In a preferred embodiment, the partially condensed first upper vapor stream 116 is partially mixed with the second reflux stream 136 and / or the absorbing liquid 140 at the reflux drum 118 or upstream of the reflux drum. Equilibrium is achieved. Thus, the first liquid reflux (part of the liquid in the partially condensed first upper vapor) is mixed with the second liquid reflux 136 and / or the absorbing liquid 140.

Generally, depending on the composition of the natural gas source, the second reflux stream 136 is less than about 20% of the total reflux (including any absorbent liquid) and the absorbent liquid 140 is less than about 10% of the total reflux. If the natural gas raw material 110 does not contain a suitable component in the absorbent liquid 140 or does not contain a sufficient amount, these components may be introduced as additional raw materials.

The second vapor stream 120 may be compressed (not shown) prior to being introduced into the main heat exchanger 122 and / or may be depressurized prior to subcooling. If the LNG product 124 is stored at high pressure (PNGL), there is no need to overcool in the cold bundle.

The main heat exchanger 122 is cooled by vaporizing the recycled mixed coolant (MR) stream 150, which is compressed and cooled by a multistage propane vaporization, liquid 152 and light vapor 156. (Compression, cooling, and phase separation are not shown). Steam 156 is condensed, cooled and expanded through throttle valve 158. Liquid 152 is mixed with condensation vapor 156 that cools, expands through throttle valve 154 and vaporizes. The mixed MR stream is completely vaporized and exits the main heat exchanger 122 as stream 150. Throttle valves 154 and / or 156 may be replaced with an isentropic concentrated fluid expander, such as a hydraulic turbine. Any other cooling system or combination of these systems, including pure fluid cascade and isentropic vapor expansion as disclosed in US-A-6308531, can be used to cool the main heat exchanger 122.

FIG. 2 illustrates a variation of the embodiment of FIG. 1, where reflux drum 118 is replaced with absorption column 218. An absorption liquid 140 and / or a second reflux stream 136, preferably a mixture of both, is fed to the top of the absorption column 218. They may also enter the column independently at the same location or at different locations along with at least one of the two streams fed to the top of the absorption column 218. For example, absorbing liquid 140 may be supplied to some stages below the top of the column or below the column. The second upper vapor stream 120 is withdrawn from the top of the column 218 and the first reflux stream 119 is withdrawn from the bottom of the column. Multiple stages in column 218 enhance the absorption of heavy components from the rising vapor.

FIG. 3 illustrates another variation of the embodiment of FIG. 1, in which the ethane rich stream 130 and the absorbing liquid 140 are combined to form a single stream 330. Stream 330 is cooled and partially condensed against propane vaporizing in heat exchanger 332, further cooled in main heat exchanger 122 to fully condensate, pumped to pressure of scrub column in pump 334 Is introduced into the reflux column. Mixing and condensing streams 130 and 140 at a higher temperature is thermodynamically more efficient than the configuration shown in FIGS. 1 and 2. The benefit is similar to that of the absorption column 218 where absorption takes place in the heat exchangers 332 and 122. In addition, this configuration does not pass through the main heat exchanger (122). As in the configuration of FIG. 1, streams 116 and 330 can be mixed downstream of main heat exchanger 122 and before reflux drum 118.

FIG. 4 illustrates a variation of the embodiment of FIG. 3 in which the ethane rich stream and the absorbing liquid stream 330 are mixed and fed to the phase separator 430. The liquid portion 438 is pumped by the pump 432 to the pressure of the scrub column 114 and mixed with the first upper vapor 116 upstream of the main heat exchanger 122. The mixed stream 416 exiting the main heat exchanger 122 is then fed to the reflux drum 118. A small amount of vapor portion 436 is condensed in the main heat exchanger 122, pumped by the pump 434, introduced into the reflux drum 118 and optionally mixed with stream 416, or the main heat exchanger ( A mixture of natural gas liquefied upstream of the supercooled portion (cold bundle) of 122, wherein the liquid may be depressurized prior to subcooling. Mixing both streams 130 and 116 and absorbing liquid 140 upstream of main heat exchanger 122 further increases the thermodynamic efficiency of the process described above.

Optionally, stream 438 may be cooled in a separate circuit in main heat exchanger 122 prior to introduction to reflux drum 118. The stream 130 contains little methane, which can be excluded from the scrub column 114 or additional demethanizer columns in the fractionation system and the stream 330 can be fully condensed and a phase separator 430 is required. If not, stream 436 will be absent and pump 434 may also be removed. In addition, stream 438 may be fed to scrub column 114 directly, such as to a second stage below the top of the column.

5 shows that the separated vapor portion 436 is compressed to the pressure of the scrub column 114 in the compressor 530 and cooled and condensed in the heat exchanger 532 and the resulting stream 536 mixes with the liquid portion 438. 4 depicts a variant of the embodiment of FIG. 4, forming stream 538. Heat exchanger 532 may be a series of heat exchangers consisting of a first heat exchanger using cooling water and other heat exchanger (s) using propane vaporizing. Stream 438 may be warmed to a temperature close to ambient temperature prior to compression in the additional heat exchanger and cooled again after being compressed in an aftercooler and the same additional heat exchanger for additional thermodynamic efficiency. Stream 536 may be concentrated supercritical fluid.

FIG. 6 shows that the first upper vapor 116 is cooled in the heat exchanger 612 and partially condensed, for example, using either or both of reflux stream 136 and absorbing liquid 140, but preferably vaporizing Another variation of the embodiment of FIG. 4 is shown, cooled by propane and partially condensed. The resulting first two-phase stream is separated in phase separator 618 into a "second" upper vapor stream 616 and a methane-rich liquid stream 619. Liquid stream 619 is returned to scrub column 114 as reflux. Stream 616, now at a temperature consistent with the temperature of the bottom of main heat exchanger 122, is mixed with stream 438 and cooled in main heat exchanger 122, reflux drum 628 as a two-phase stream 626. Supplied to. Upper vapor stream 620 from reflux drum 628 is liquefied in main heat exchanger 122 and recovered as liquefied natural gas product 124. Liquid stream 629 from reflux drum 628, which is optionally reheated in main heat exchanger 122, is returned to scrub column 114 at the same or different location as reflux stream 619.

Phase separator 618 and / or reflux drum 628 may be replaced with an absorption column having a two-phase source at the bottom, reflux provided at the top by cooled streams 136 and / or 140.

Individual features or combinations of these features described above in connection with any of the illustrated embodiments may be suitably incorporated in any of the other embodiments shown. For example, selectively reheating the reflux stream 629 in the main heat exchanger 122 as described above with respect to FIG. 6 may be applied to any of the embodiments of FIGS. 1-5. Additionally or alternatively, providing reflux to scrub column 114 by liquid portion 619 branched from first upper vapor 116 of the embodiment of FIG. 6 may also be any of the embodiments of FIGS. 1-5. It can be applied to the embodiment of.

Yes

Using the embodiment of FIG. 3, the pre-purified natural gas stream 110 of 950 psia (6.5 MPa) and 97,904 lbmol / h (44,408.5 kgmol / h) was propane in three stages up to -32.3 ° F (-35.7 ° C). By cooling, it is cooled in the heat exchanger 112 and supplied to the scrub column 114. This feed stream 110 comprises 0.6% nitrogen, 84.8% methane, 7.3% ethane, 4.4% propane, 0.7% isobutane, 1.5% butane, 0.3% isopentane, 0.2% pentane, and 0.2% hexane. The column 114 operates at 840 psia (5.8 MPa) and is about 130 ° F. (55 ° C.) and an intermediate reboiler heated by 40% of the stream 110 bypassing the second stage propane cooling. And a lower reboiler 128. The column top layer 116 is cooled from -62.3 ° F. (-52.4 ° C.) to -77.5 ° F. (-60.8 ° C.) in the warmed bundle of the main heat exchanger 122 and as a two-phase stream containing about 15% liquid. Is introduced into the reflux drum 118. The bottoms stream 126 of the scrub column is sent to a fractionation system 128 having a series of distillation columns consisting of a deethane group, a depropane group, and a debutane group. 96% of the propane present in feed stream 110 is recovered as depropane top layer. Almost all butane and isobutane are recovered as the debutane group upper layer. The upper layer of deethane containing about 39% methane, 61% ethane and only 0.05% propane was 39% at a flow rate of 6,105 lbmol / h (2,769 kgmol / h) and a pressure of 420 psia (2.9 MPa) Is mixed with stream 140 consisting of the bottom butane group bottom liquid of and the residue recovered as C ₅₊ product. Low propane content is important for high propane recovery. Stream 140 is a liquid at a pressure of 17 psia (117 kPa) and a flow rate of 406 lbmol / h (184 kgmol / h), about 51% isopentane, 36% pentane, 12% hexane and less than 1% Contains hard components. The stream is pumped to 420 psia (2.9 MPa) by a pump not shown in FIG. 3 prior to mixing with the ethane rich stream 130. Mixed stream 330 is cooled by propane to -32.3 ° F. (-35.7 ° C.) in heat exchanger 332 and further up to −77.5 ° F. (-60.8 ° C.) in a warmed bundle of main heat exchanger 122. By cooling it completely condenses. The condensed stream is pumped from the pump 334 to the pressure of the scrub column and introduced into the reflux drum 118. Liquid reflux 119 is returned to the top of scrub column 114 at a temperature of -74.2 ° F. (-59.0 ° C.), with a heat effect due to pumping and mixing in the phase separator. The temperature of stream 120, which contains 91.3% methane, 7.8% ethane, 0.7% nitrogen, 0.2% propane, and a very small amount of heavy hydrocarbons, is -74.2 ° F. (-59.0 ° C.) and the flow rate of this stream is 83,571. lbmol / h (37,907 kgmol / h). This stream is cooled to −161.6 ° F. (−107.6 ° C.) in a cold bundle at the center of the main heat exchanger 122 and then has a storage pressure of 15.3 psia (105.5 kPa) as the liquid stream 124. As described above with reference to FIG. 1, the main heat exchanger 122 is cooled by a mixed coolant made of nitrogen, methane, ethane, and propane.

It is to be understood that the invention is not limited to the foregoing description with reference to the preferred embodiments and that modifications and variations can be made without departing from the scope of the invention as defined by the following claims.

Claims (41)

As an integrated process for producing natural gas liquid (NGL) and liquefied natural gas (LNG) from natural gas sources of methane mixed with ethane and heavy hydrocarbon (s), Introducing a natural gas source into the scrub column at a first location; Extracting from the scrub column a first upper vapor stream subtracting a component heavier than methane and a bottoms stream enriched in components heavier than methane; Cooling and partially condensing the first upper vapor stream to form a first biphasic stream; Separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane; Introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location; Liquefying a second upper vapor stream in a main heat exchanger to provide LNG product; Separating the bottoms stream into an ethane rich stream and an NGL product stream richer in ethane than ethane; Fully condensing the ethane rich stream in the main heat exchanger at a temperature below the temperature of the natural gas feed to the scrub column; And Pumping the condensed stream as a second reflux stream to the scrub column at a location selected from a second location and a third location above the first location. Integration process comprising a. The process of claim 1 wherein the coolant for the main heat exchanger is a recycled mixed coolant. The process of claim 1, wherein the methane-rich first reflux stream comprises at least 80% of the total reflux (ie, the liquid fed to the scrub column above the first location). The process of claim 1, wherein the second reflux stream is less than 20% of the total reflux (ie, the liquid fed to the scrub column above the first location). The process of claim 1 or 2, wherein the cooling and partial condensation of the first upper vapor stream is performed in a warmed bundle of the main heat exchanger. The process of claim 1 or 2, wherein the ethane-rich second reflux stream is fed to the scrub column separately from the methane-rich first reflux stream. The process of claim 1 or 2, wherein the ethane-rich second reflux stream is mixed with the methane-rich first reflux stream prior to entering the scrub column. 8. The process of claim 7, wherein the ethane-rich second reflux stream is mixed with the first two-phase stream at a location selected upstream of the reflux drum and at the reflux drum. 8. The process of Claim 7, wherein the first two-phase stream is fed to the bottom of the absorption column where a second reflux stream enriched in ethane is supplied as reflux. 8. The process of Claim 7, wherein the ethane rich stream is fully condensed before the methane is mixed with the rich first reflux stream. The integrated process according to claim 1 or 2, wherein the ethane rich stream is the upper vapor of the deethane group. 3. The scrub column according to claim 1 or 2, wherein the absorbent liquid obtained from at least one stream enriched in constituents heavier than ethane is selected from the second, third and fourth positions above the first position. To be introduced into the integration process. The process of claim 12, wherein the absorbing liquid comprises pentane and isopentane. The process of claim 12, wherein the absorbent liquid comprises C ₄ hydrocarbon (s). The process of claim 12, wherein the absorbing liquid comprises C ₅₊ hydrocarbon (s). The process of claim 12, wherein the absorbing liquid is fed to the scrub column separately from one of the second reflux stream enriched in ethane or the first reflux stream enriched in methane. The process of claim 12, wherein the absorbent liquid is mixed with at least one of a methane rich first reflux stream and an ethane enriched second reflux stream prior to entering the scrub column. 18. The process of claim 17, wherein the absorbing liquid is mixed with at least one of the first two-phase stream and the ethane-rich second reflux stream at selected locations upstream of the reflux drum and at the reflux drum. 18. The process of claim 17, wherein the first two-phase stream is fed to the bottom of the absorption column where at least one of the absorption liquid and the ethane-rich second reflux stream is supplied as reflux. The process of claim 19, wherein the absorbing liquid is mixed with the first upper vapor stream prior to partially condensing the first upper vapor stream to form a first two-phase stream. The process of claim 12, wherein the absorbing liquid is mixed with the gaseous ethane rich stream prior to condensing the gaseous ethane rich stream to provide a second reflux stream. The process of claim 21, wherein the mixed sorbent liquid and the gaseous ethane rich stream are phase separated and the liquid portion is fed to the scrub column above the first location. The process of claim 22, wherein the vapor portion is condensed and fed to the scrub column above the first location. The process of claim 22, wherein the liquid portion is mixed with the first upper stream prior to partially condensing the upper stream to provide a first two-phase stream. The process of claim 22, wherein the condensed vapor portion is mixed with the first upper stream prior to partially condensing the upper stream to provide a first two-phase stream. The process of claim 12, wherein the absorbing liquid comprises less than 10% of the total reflux (ie, the liquid supplied to the scrub column above the first location). The process of claim 1, wherein the second reflux stream comprises less than 0.05% propane. The process of claim 1, wherein the methane can be removed from the ethane rich stream so that the second reflux stream comprises ethane. A production apparatus for producing natural gas liquid (NGL) and liquefied natural gas (LNG) from a natural gas source of methane mixed with ethane and heavy hydrocarbon (s) by an integrated process according to claim 1, Scrub column 114; Conduit means (110) for introducing a natural gas feed into the scrub column at a first location; Conduit means 116 for withdrawing a scrub column from the first upper vapor stream subtracting the component heavier than methane and the bottom stream 126 enriched in the component heavier than methane; Heat exchange means (122) for cooling and partially condensing the first upper vapor stream to form a first two-phase stream; Separating means (118; 218) for separating the first two-phase stream to provide a second upper vapor stream and a first reflux stream enriched in methane; Conduit means (119) for introducing a first reflux stream enriched in methane at a second location of the scrub column above the first location; A main heat exchanger 122 for liquefying a second upper vapor stream to provide LNG product 124 and for completely condensing the ethane rich stream at a temperature below the temperature of the natural gas feed to the scrub column; Separating means 128 for separating the bottoms stream into an ethane rich stream and an NGL product stream richer in ethane than ethane; Conduit means (130) for supplying an ethane rich stream to the main heat exchanger; Conduit means (136 and 119) for introducing the ethane rich stream condensed at a position selected from a second position above the first position and a third position as a second reflux stream to the scrub column; And Pumping means 134 for pumping the condensed ethane rich stream before being introduced into the scrub column 114. Production apparatus comprising a. 30. The production apparatus of claim 29, wherein the heat exchange means for cooling and partially condensing the first upper vapor stream is a warmed bundle of a main heat exchanger. 31. The production apparatus according to claim 29 or 30, wherein the production apparatus comprises a reflux drum 118 wherein a mixture of a ethane enriched second reflux stream and a methane enriched first reflux stream is obtained from the reflux drum. 114) a production apparatus. 31. The production apparatus according to claim 29 or 30, wherein the production apparatus comprises an absorption column 218, which receives the first two-phase stream as a bottom feed and the ethane-rich second reflux stream as reflux. And a bottom liquid from said absorption column is supplied to a scrub column. 31. The method of claim 29 or 30, wherein at a selected position of the second, third, and fourth positions above the first position, the component (s) is heavier than ethane and is enriched for separating the bottom stream of the scrub column. And conduit means (140, 136 and 119) for introducing the absorbent liquid provided by the separating means (128) into the scrub column (114). 34. The apparatus of claim 33, wherein the production apparatus comprises a reflux drum 118, wherein a mixture of the absorbing liquid and at least one of the first reflux stream enriched with methane and the second reflux stream enriched with ethane is from the reflux drum. The production apparatus being fed to the scrub column (114). 34. The apparatus of claim 33, wherein the production apparatus comprises an absorption column 218, which receives the first two-phase stream as a bottom feed and at least one of the absorption liquid and a second reflux stream enriched in ethane as reflux. And a bottom liquid is supplied to the scrub column from the absorption column. 34. The production apparatus of claim 33, comprising mixing means 438 for mixing the absorbing liquid with the first upper vapor stream prior to partially condensing the first upper vapor stream to form a first biphasic stream. . 34. The production apparatus according to claim 33, comprising mixing means (140 and 330) for mixing the absorbing liquid with the gaseous ethane rich stream prior to condensing the gaseous ethane rich stream to provide a second reflux stream. 38. The separator according to claim 37, comprising: separator means (430) for phase separation of the mixed sorbent liquid and gaseous ethane rich stream, and conduit means (438 and 416) for feeding the liquid portion to the scrub column (114) above the first location. Production apparatus). The heat exchange means (122; 532) for condensing the vapor portion, and conduit means (436; 536, 538, and 516) for supplying the condensed vapor to the scrub column (114) above the first location. Production apparatus comprising a. 39. An apparatus according to claim 38, comprising mixing means (438) for mixing the liquid portion with the first upper stream prior to partially condensing the first upper stream to provide a first two-phase stream. 40. The method of claim 39, comprising mixing means 532 and 538 for mixing the condensed vapor portion with the first upper stream prior to partially condensing the first upper stream to provide a first two-phase stream. Production device.

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