METHODS AND CONFIGURATION FOR RETROFITTING NGL PLANT FOR HIGH ETHANE RECOVERY

Abstract

A natural gas liquid plant is retrofitted with a bolt-on unit that includes an absorber that is coupled to an existing demethanizer by refrigeration produced at least in part by compression and expansion of the residue gas, wherein ethane recovery can be increased to at least 99% and propane recovery is at least 99%, and where a lower ethane recovery of 96% is required, the bolt-on unit does not require the absorber, which could be optimum solution for revamping an existing facility. Contemplated configurations are especially advantageous to be used as bolt-on upgrades to existing plants.

Description

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

Not applicable.

REFERENCE TO A MICROFICHE APPENDIX

Not applicable.

BACKGROUND

Natural gas liquids (NGL) may describe heavier gaseous hydrocarbons: ethane (C2H6), propane (C3H8), normal butane (n-C4H10), isobutane (i-C4H10), pentanes, and even higher molecular weight hydrocarbons, when processed and purified into finished by-products. Systems can be used to recover NGL from a feed gas using natural gas liquids plants.

SUMMARY

In an embodiment, a natural gas liquid plant bolt-on unit may comprise an absorber configured to condense the ethane content from an overhead gas stream from a demethanizer using a cold lean residue gas to produce a liquid portion and a vapor portion, wherein the liquid portion is configured to provide a reflux to the demethanizer, and the vapor portion is configured to provide cooling of a reflux exchanger and a subcooler; and a flow control valve configured to pass about 70% to 90% of the vapor portion to reflux cooling and reflux of the demethanizer in the subcooler.

In an embodiment, a method may comprise passing an overhead vapor stream from a demethanizer to an absorber; contacting the overhead vapor stream with a cold lean residue gas to produce a liquid portion and a vapor portion within the absorber; passing the liquid portion back to the demethanizer as reflux; and passing the vapor portion to a subcooler, wherein the subcooler cools at least a first portion of the vapor portion to produce the cold lean residue gas.

In an embodiment, a method may comprise passing an overhead vapor stream from a demethanizer to a first heat exchanger; cooling a compressed cooled residue gas using at least a first portion of the overhead vapor stream from the demethanizer in the first heat exchanger; compressing the first portion of the overhead vapor stream downstream of the first heat exchanger to produce a compressed vapor portion; cooling the compressed vapor portion to produce the compressed cooled residue gas that passes to the first heat exchanger; passing the compressed cooled residue gas to a pressure reduction device to produce a cold lean residue gas; and passing the cold lean residue gas to the demethanizer as reflux.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of the present disclosure, reference is now made to the following brief description, taken in connection with the accompanying drawings and detailed description, wherein like reference numerals represent like parts.

FIG. 1 illustrates a typical NGL plant.

FIG. 2 illustrates a bolt-on unit for use with an NGL plant.

FIG. 3 is the heat composite curve of a reflux exchanger.

FIG. 4 is the heat composite curve of a feed exchanger and a subcool exchanger.

FIG. 5 illustrates a bolt-on unit with a revamped demethanizer for use with an NGL plant.

FIG. 6 illustrates a bolt-on unit utilizing an existing residue gas compressor for use with an NGL plant.

FIG. 7 illustrates a bolt-on unit utilizing an existing residue gas compressor requiring no changes to equipment in the existing facility for use with an NGL plant.

FIG. 8 illustrates a bolt-on unit requiring minor modifications to the existing demethanizer for use with an NGL plant.

DETAILED DESCRIPTION

It should be understood at the outset that although illustrative implementations of one or more embodiments are illustrated below, the disclosed systems and methods may be implemented using any number of techniques, whether currently known or not yet in existence. The disclosure should in no way be limited to the illustrative implementations, drawings, and techniques illustrated below, but may be modified within the scope of the appended claims along with their full scope of equivalents.

The following brief definition of terms shall apply throughout the application:

The term “comprising” means including but not limited to, and should be interpreted in the manner it is typically used in the patent context;

The phrases “in one embodiment,” “according to one embodiment,” and the like generally mean that the particular feature, structure, or characteristic following the phrase may be included in at least one embodiment of the present invention, and may be included in more than one embodiment of the present invention (importantly, such phrases do not necessarily refer to the same embodiment);

If the specification describes something as “exemplary” or an “example,” it should be understood that refers to a non-exclusive example;

The terms “about” or “approximately” or the like, when used with a number, may mean that specific number, or alternatively, a range in proximity to the specific number, as understood by persons of skill in the art field; and

If the specification states a component or feature “may,” “can,” “could,” “should,” “would,” “preferably,” “possibly,” “typically,” “optionally,” “for example,” “often,” or “might” (or other such language) be included or have a characteristic, that particular component or feature is not required to be included or to have the characteristic. Such component or feature may be optionally included in some embodiments, or it may be excluded.

All references to percentages of flow refer to volumetric percentages unless otherwise indicated.

The field of the present disclosure is natural gas liquids plants, and especially relates to retrofitting natural gas liquids plants for high ethane recovery. The present systems and methods relate to the recovery of ethane, propane, and heavier hydrocarbons from the natural gas stream. A typical shale gas may contain 78% methane, 9% ethane, 5.8% ethane, and the balance butane and heavier hydrocarbons, as shown below in Table 1.

Heat and Material Balance
Stream Description	Feed Gas	Demethanizer Overhead	Reflux to Absorber	Absorber bottom	Residue Gas	NGL
Stream Number	1	11	69	64	17	12
Mole %
N2	0.52	0.58	0.66	0.18	0.66	0.00
C1	77.84	98.05	99.19	92.56	99.19	0.40
C2	8.94	1.30	0.15	6.86	0.15	50.17
C3	5.78	0.07	0.00	0.38	0.00	32.85
IC4	0.81	0.00	0.00	0.01	0.00	4.60
NC4	1.40	0.00	0.00	0.01	0.00	7.96
IC5	0.25	0.00	0.00	0.00	0.00	1.42
NC5	0.30	0.00	0.00	0.00	0.00	1.70
C6	0.11	0.00	0.00	0.00	0.00	0.63
C7	0.04	0.00	0.00	0.00	0.00	0.23
C8	0.01	0.00	0.00	0.00	0.00	0.06
Pressure, psig	1.153	445	470	445	654	447
Temperature, °F	77	-129	-141	-134	120	110
Flow, MMscfd	199.6	189.0	52.3	32.6	156.5	35.1

The richness of the feed gas and its high liquid content would potentially generate revenue from gas processing. However, due to the cyclic price fluctuation of natural gas and the natural gas liquids (NGLs), especially ethane liquid, gas processors must decide on the optimum level of NGL recovery that makes economic sense. Consequently, there is a demand for processes that require low capital investment that can also be upgraded for higher recoveries when the price ofNGLs becomes more attractive in the future. Therefore, there are needs for efficient recoveries of these products and processes that can provide efficient recoveries with lower capital investment. Available processes for separating these materials include those based upon cooling and refrigeration of gas, such as oil absorption and/or refrigerated oil absorption. Additionally, cryogenic processes have gained popularity because of the availability of advanced turbo-expander equipment to produce power while generating refrigeration for the cryogenic process.

The cryogenic expansion process is now generally preferred for natural gas liquids recovery because it provides flexibility, efficiency, and reliability. There are numerous patented processes that can be used to meet the varying degrees of recovery.

Most of the NGL recovery processes are based on the use of feed gas in refluxing the absorber. These processes are simple with an ease of operation and have low equipment counts. The relatively low investment can be justified by the NGL produced. These plants are based on the feed gas reflux process coupled with turbo-expander for cooling and power production and can achieve 70% to 80% ethane recovery. The level of recovery depends on a number of factors including feed gas composition, feed gas supply pressure, and/or availability of refrigeration.

To meet ethane recovery higher than 80%, reflux processes using lean residue gas can be used. The residue gas is compressed to a higher pressure, cooled and expanded to generate deep cooling to the demethanizer. However, these processes require additional compression and heat exchanger equipment that must be justified by the additional NGL production. In most cases, the power for recycle compression cannot justify the revenues from additional production, especially when ethane values remain unattractive.

However, with improving pricing of the ethane commodity as a feedstock to petrochemical plants, there is a drive for gas processors to produce ethane liquid for sales. Existing plants can be retrofitted with residue gas reflux, such as U.S. Pat. number 8,910,495 to Mak. Such modification would require re-engineering of the existing system which would require significant capital investment. The plant revamp also requires extensive shutdown of the existing facility, which will result in revenue losses from liquid and gas production. In most instances, an extensive revamp of the existing facility cannot be justified for the increase in NGL production.

The contemplated systems and methods present an economical and effective solution that can be implemented with the existing facility to increase ethane recovery from current levels to about or greater than 95% and most preferably 99% using an add-on (or bolt-on) unit that can eliminate extensive downtime of the facility. Any unit that is described as an “add-on” unit may in some embodiments comprise a unit that can be connected to (e.g., bolted onto, etc.) the existing units, which can be referred to as a “bolt-on” unit.

From a green field installation standpoint, the NGL recovery process can be designed with a moderate ethane recovery process, while investment of the bolt-on unit for high recovery can be deferred until the ethane market becomes more attractive. This approach will conserve capital for the project by delaying investment for high recovery to the future.

FIG. 1 illustrates a typical NGL process employed by the gas processing industry for recovering ethane NGL, known as the gas subcooled process (also known as the GSP process). As shown in FIG. 1, a dried feed gas stream 1, typically at about 800 to 1000 psig and about 80 to 100° F., can be cooled by a cold residue gas stream 15 in feed exchanger 40, forming stream 2. Stream 2 may be further cooled by propane refrigeration in chiller exchanger 41, forming stream 3, typically at -25 to -30° F. The two phase stream 3 may be separated in cold separator 42 into a vapor stream 4 and a liquid stream 43. The vapor stream 4 from the separator 42 can be split into two portions; stream 7 and stream 6.

In the GSP process, the flow ratio of stream 7 to the total flow (stream 4) is typically controlled at about 66% to turbo-expander 44 by a flow ratio controller 70. Stream 7 can be expanded across the turbo-expander 44 to provide a cooling stream 18 to the demethanizer 49. The remaining flow, stream 6, is cooled in the subcool exchanger 46 by the cold residue gas stream (or overhead gas stream) 11 to form a subcooled liquid stream 14 (which may be also known as a reflux stream 14) at about -130 to -150° F., which is further letdown in pressure in a Joule Thomson (JT) valve 47, producing a cold reflux stream 71 to the demethanizer 49. Flashed liquid stream 43, from cold separator 42, is fed to the lower section of the demethanizer 49, where the demethanizer column 49 typically operates at about 210 to 350 psig. The demethanizer 49 may be heated with a side reboiler using a column side-draw, stream 8, in feed exchanger 40, and a bottom reboiler 48. The NGL product in the demethanizer 49 is heated to remove its methane content to meet the 1 volume % methane specification. The demethanizer 49 produces an overhead gas stream 11, and an ethane rich NGL stream 12. The overhead gas stream 11 passes through subcool exchanger 46, producing stream 15, and feed exchanger 40, producing stream 16 which is further compressed by compressor 45 using power generated by turbo-expansion, producing residue gas stream 17.

Such configurations can recover 80% to 88% of the ethane content in the feed gas; the recovery levels depend on the feed gas composition, feed supply pressure, and demethanizer pressure. While lowering the demethanizer pressure can increase ethane recovery, the end result is marginal and is typically not justified due to the high gas compression cost.

Thus, although various configurations and methods for higher ethane recovery from natural gas are known in the art, all or almost all of them suffer from one or more disadvantages. Therefore, there is still a need for configurations and methods for ethane recovery, especially in retrofitting an NGL plant.

The present systems and methods are directed to retrofitting natural gas liquid plants with a bolt-on unit that can increase ethane recovery from the current levels to at or above about 95%, and most preferably at or above about 98% to 99%. As used herein, a bolt-on unit can include a unit that is intended to be added to an existing unit to retrofit the existing configuration. While referred to as a bolt-on unit, such a unit may not physically require bolts or be limited to simply being connected onto an existing unit without changing the flow configuration. In addition, the term bolt-on unit can also refer to a portion of a new unit being constructed from scratch.

The contemplated process includes an absorber operating at between about a 10° F. to about a 20° F. lower temperature than the existing demethanizer, typically at -165 to -170° F., using compression and expansion of the residue gas as the reflux to the absorber.

In one aspect, the absorber receives feed gas from the existing demethanizer, condenses its ethane content by refluxing with the cold residue gas to produce a lean overhead and a bottom ethane rich liquid that, in turn, is used as reflux to the existing demethanizer.

In another aspect, the absorber produces a residue gas that is compressed, cooled, condensed, and subcooled, producing a cold lean reflux liquid to be used in the absorber.

In another aspect, where the facility has limited space to allow installation of a new absorber, the cold lean reflux liquid is mixed with the feed gas reflux from the existing demethanizer, and fed to the demethanizer as a combined reflux, eliminating the need for a new absorber. This configuration requires minimum down-time for the installation of one heat exchanger, and does not require modification of the existing demethanizer. This process can achieve an ethane recovery of at least about 97%.

In yet another aspect, where the demethanizer can be revamped in a way that allows for feeding the cold lean reflux liquid to the top tray, which is installed at least 4 trays above the existing feed gas reflux tray, ethane recovery can be increased up to about 99%. This configuration may require some downtime for modification of the existing demethanizer column, but the higher ethane recovery may justify the downtime and cost on revamping the demethanizer.

From another perspective, the process can employ a refluxed absorber located downstream of the existing demethanizer to recover the residual ethane and propane from the feed gas, which can improve ethane recovery from 80% up to about 99% and propane recovery from 95% up to about 99%.

From another perspective, the process employs a high pressure recycled cold reflux stream that is mixed with feed gas reflux to the existing demethanizer, to lower the reflux temperature, allowing ethane recovery to be improved from 80% up to about 97%, without changes to the existing demethanizer. Where revamping the existing demethanizer is a viable option, the recycle cold reflux stream can be fed as a top reflux to the existing demethanizer, further improving ethane recovery up to 99%.

In another contemplated system, the absorber overhead vapor is first used to cool the compressed residue gas (cold end) to produce a cold reflux to the absorber, and then split into two portions. About 10% to about 30% can be used to cool the compressed residue gas (warm end) and the remaining portion of about 70% to about 90% can be used to cool the feed gas in the subcool exchanger in the existing unit. The split flow ratio can be adjusted as needed to meet the ethane recovery levels.

The following figures describe embodiments of the bolt-on unit configured to increase ethane recovery of an existing NGL plant from the current levels, typically at about 80% to 90%, to a higher recovery of up to about 95%, or preferably up to about 98%, or most preferably up to about 99% ethane recovery.

An embodiment of a bolt-on unit 100 is depicted in FIG. 2. The bolt-on unit 100 may be used with the system as described in FIG. 1, where only the new parts of the system are described below. The remaining portions can be the same as or similar to those described with respect to the elements shown in FIG. 1, and the description of those elements is hereby repeated. As shown in FIG. 2, the feed stream to the bolt-on unit 100 is the overhead gas stream 11 from existing demethanizer 49.

Stream 11 can be routed to absorber 84 in which a residue gas stream 69 (which may also be known as a reflux stream 69 to the absorber 84) is letdown in pressure and cooled, providing a reflux stream to the absorber 84. As is generally known, an absorber provides contact between a rising vapor phase and a falling liquid phase with heat and mass transfer between the two phases along the length of the absorber. The absorber 84, operating at a pressure slightly lower than the demethanizer 49, can produce an overhead vapor stream 62 and a bottom liquid stream 64. The bottom ethane rich liquid stream 64 can be pumped by pump 85 forming stream 65 which can be mixed with the cold reflux stream 71 from subcool exchanger 46 and fed as a combined reflux 72 to the demethanizer 49. In some embodiments, the stream 65 can be introduced into the demethanizer 49 as a stream separate from the cold reflux stream 71.

The refrigerant content in the absorber overhead vapor stream 62 can be recovered in an efficient manner, with the cold end of the heat release curve used to cool the residue gas stream 69 in reflux exchanger 82 to produce the low temperature reflux stream 61 to the absorber 84, while the warm end of the heat release curve is used to cool the warm end of the residue gas cooling curve, and to cool the feed gas stream 15 to provide reflux to the demethanizer 49.

The portion 66 (i.e. heated absorber vapor stream 66) of the absorber overhead vapor stream 62 passing to the recycle compressor 80 can be controlled at about 10% to about 30% of total flow (flow ratio of stream 66 to stream 62) using a flow ratio controller 70. The remaining portion 91 of the absorber overhead vapor stream 62 can be about 70% to about 90% of the absorber overhead vapor stream 62, and the remaining portion 91 may be routed through exchangers 46 and 40 and further compressed by compressor 45 using power generated by turbo-expansion, producing residue gas stream 17.

The effective heat release curves are shown in FIG. 3 for the reflux exchanger 82 and FIG. 4 for the feed and subcool exchangers 40 and 46 in the configurations they are shown in FIG. 2.

The heated absorber vapor stream 66 can be compressed by compressor 80 to form the high pressure stream 67, which is cooled in air cooler 81 to form stream 68 and further cooled in reflux exchanger 82 to form residue gas stream 69. The cold, high pressure residue gas stream 69 can be letdown in pressure in a JT valve 83 to produce the lean reflux stream 61 to the absorber 84.

As an example of suitable conditions of the process shown in FIG. 2, the demethanizer 49 can operate at about 230 to about 350 psig and at a temperature between about -125 to about -165° F. The non-bolt-on portion of the NGL plant can be designed to process an inlet feed gas flow of about 200 million metric standard cubic feet per day (MMscfd) and recover about 80% of its ethane content. The residue stream 69 can be letdown to about 230 to 250 psig and cooled, providing the reflux stream to the absorber 84. The absorber 84, which can operate at a pressure slightly lower than the demethanizer 49, can produce an overhead vapor stream 62 at about -140° F. to -175° F. and a bottom liquid stream 64. The heated absorber vapor stream 66, which can be at about 100° F., can be compressed by compressor 80 to about between about 1200 psig to about 1500 psig to form the high pressure stream 67.

FIG. 5 provides an alternate configuration of a bolt-on unit 500 that can reduce the cost of the bolt-on unit 500 by integrating the functionality of the absorber system into the demethanizer 49. The bolt-on unit 500 may be used with the system as described in FIG. 1 and/or FIG. 2, where only the new parts of the system are described below, and the description of the elements shown in FIG. 1 is hereby repeated. This alternative can eliminate the absorber 84 and reflux pump 85 (described in FIG. 2), providing the existing demethanizer column 49 can be revamped for the higher throughput. The remaining components can be the same or similar to those components described with respect to FIG. 2. The low temperature reflux stream 61 may be fed directly to the demethanizer 49, and the overhead gas stream 11 may be fed directly to the reflux exchanger 82. Additionally, the reflux stream 61 may not be combined with the reflux stream 71 before it is fed to the demethanizer 49. This alternative can recover up to about 99% ethane. In some embodiments, the existing demethanizer 49 can be modified to include a reflux nozzle for the reflux stream 61 when the reflux stream 61 is injected directly into the demethanizer 49. This alternative can reduce the equipment count and the capital and installation cost of the bolt-on unit 500.

Referring to FIG. 6, in some embodiments, the residue gas stream 17a (as described as stream 17 in FIG. 1) may be further compressed using a residue gas compressor 680. The bolt-on unit 600 may be used with the system as described in FIG. 1 and FIG. 2, where only the new parts of the system are described below, and the description of the elements shown in FIG. 1 is hereby repeated. This residue gas stream 17a from the existing unit can be mixed with the heated absorber vapor stream 66 from the bolt-on unit 600. FIG. 6 provides an alternate configuration where the residue gas compressor 680 has extra capacity, and the compressor 680 can be used for the gas recycle function, avoiding the need for a new gas compressor 80 (as described in FIGS. 2 and 3), which would improve the economics of the installation. The higher ethane recovery would also result in a reduction in the ethane component in the residue gas which would free up capacity for gas recycling.

The bolt-on unit 600 may comprise the recycle reflux exchanger 82, absorber 84 and pump 85, as described above in Figured 2. The high-pressure residue gas compressor 680 may produce stream 67 which may be cooled by air cooler 81, producing discharge stream 68 which is split into two portions as described more herein. A first portion having about 8 to 15% (recycle stream 68b) can be routed to reflux exchanger 82, cooled and condensed to form residue gas stream 69, which is then letdown in pressure in valve 83 producing a reflux stream 61, and fed to the absorber 84. The operating pressure of the absorber 84 can depend on the operating pressure of the existing demethanizer 49. The absorber 84 is fed by the overhead gas stream 11 from the demethanizer 49, and can produce an ethane depleted overhead vapor stream 62 and a bottom ethane rich liquid stream 64. The bottom liquid can be pumped by pump 85 to form stream 65, which can be mixed with the reflux stream 71 from subcool exchanger 46 and fed as a combined reflux 72 to the demethanizer 49. The absorber overhead vapor stream 62 can be split into two portions: stream 62a and 62b. About 10 to 30% of absorber overhead vapor stream 62 can be used to form stream 62a, which provides cooling to the recycle stream 68b. The other stream 62b, at about 70% to 90% of absorber overhead vapor stream 62, can be fed to subcool exchanger 46 producing stream 15, which can be fed to feed exchanger 40 to produce stream 16. Stream 16 can be further compressed by compressor 45 using power generated by turbo-expansion to produce product gas stream 17a. The heated absorber vapor stream 66 can be combined with stream 17a, forming stream 17b, which can be compressed by compressor 680 to form the high pressure stream 67, which can be cooled in air cooler 81 to form stream 68. Stream 68 may be split, forming the recycle stream 68b (the first portion of the high-pressure residue gas compressor discharge stream, as described above) and the product residue gas stream 68a. With this configuration, up to or over about 99% of the ethane content from the feed gas can be recovered.

As an example of suitable conditions of the process shown in FIG. 6, the first portion (recycle stream) 68b of the discharge stream 68 can be routed to reflux exchanger 82, cooled and condensed to between about -115° F. to -135° F. to form residue gas stream 69, which is then letdown in pressure in valve 83 to produce the reflux stream 61, at about -160° F. to -175° F. The operating pressure of the absorber 84 can be between about 200 to 350 psig. The demethanizer 49 can operate at about -160° F., and can produce the ethane depleted overhead vapor stream 62 at about -170° F. The heated absorber vapor stream 66, which can be at about 60 to 100° F., can be combined with stream 17a, forming stream 17b, which can be compressed by compressor 680 to about between about 850 psig to about 1200 psig to form the high pressure stream 67, which can be cooled in air cooler 81 to form stream 68. With this configuration, up to or over about 99% of the ethane content from the feed gas can be recovered.

FIG. 7 illustrates an alternate configuration of the bolt-on unit 600 described above in FIG. 6 that can reduce the cost of the bolt-on unit 700 by removing the absorber 84 and bottom pump 85. The bolt-on unit 700 may be used with the systems as described in the preceding Figures, where only the new parts of the system are described below, and the description of the previously described elements is hereby repeated. Where about 95% to 97% ethane recovery is the recovery target, the absorber and bottom pump may not be required, which would simplify the process, and would reduce the capital cost. Therefore, the bolt-on unit 700 may comprise the reflux exchanger 82, as shown in FIG. 7. In this configuration, the reflux stream 69 (i.e. the residue gas stream 69) from reflux exchanger 82 can be letdown in pressure, mixed with the reflux stream 71, and fed to the demethanizer 49 as a combined reflux stream 72. The split ratio of the recycle stream 68b to the total stream 68 (as described with respect to FIG. 6) can be maintained at between about 8% to 15%, and the split ratio of the demethanizer overhead stream 62a to the total absorber overhead vapor stream 62 (as described with respect to Figured 6) can be maintained at between about 10% to 30%. With the arrangement shown in FIG. 7, no change is required to the demethanizer 49.

FIG. 8 illustrates an alternate configuration that can reduce the cost of the bolt-on unit (relative to the bolt-on unit 600 described in FIG. 6) by removing the absorber 84 and bottom pump 85 and by integrating the absorber system into the demethanizer 49. The bolt-on unit 800 may be used with the systems as described in the preceding Figures, where only the new parts of the system are described below, and the description of the previously described elements is hereby repeated. This alternative can recover up to about 99% ethane. The existing demethanizer 49 can be modified for installation of a reflux nozzle for the recycle gas lean reflux stream 61. In this option, the existing demethanizer 49 can be revamped to add rectification trays, as shown in FIG. 8.

In the configuration of FIG. 8, the reflux stream 69 (i.e. residue gas stream 69) from reflux exchanger 82 can be letdown in pressure and fed to the top of the demethanizer 49 while the feed gas reflux stream 71 is fed to the lower section of the demethanizer 49 at about the fourth tray below the top tray. The split ratio of the recycle stream 68b to the total stream 68 (as described with respect to FIG. 6) can be maintained at about 8% to 15%, and the split ratio of the demethanizer overhead stream 62a to the total overhead vapor stream 62 (as described with respect to Figured 6) can be maintained at about 10% to 30%.

Thus, specific embodiments and applications of retrofit of NGL plant configurations for up to about 96% to 99% ethane recovery have been disclosed. It should be apparent, however, to those skilled in the art that many more modifications besides those already described are possible without departing from the inventive concepts herein. The inventive subject matter, therefore, is not to be restricted except in the spirit of the appended claims. Moreover, in interpreting both the specification and the claims, all terms should be interpreted in the broadest possible manner consistent with the context. In particular, the terms “comprises” and “comprising” should be interpreted as referring to elements, components, or steps in a non-exclusive manner, indicating that the referenced elements, components, or steps may be present, utilized, or combined with other elements, components, or steps that are not expressly referenced.

Having described various devices and methods herein, exemplary embodiments or aspects can include, but are not limited to:

In a first embodiment, a natural gas liquid plant bolt-on unit may comprise an absorber configured to condense the ethane content from an overhead gas stream from a demethanizer using a cold lean residue gas to produce a liquid portion and a vapor portion, wherein the liquid portion is configured to provide a reflux to the demethanizer, and the vapor portion is configured to provide cooling of a reflux exchanger and a subcooler; and a flow control valve, wherein the flow control valve is configured to pass about 10% to about 30% of the vapor portion to provide cooling to the absorber in the reflux condenser, and about 70% to 90% of the vapor portion to reflux cooling and reflux of the demethanizer in the subcooler.

A second embodiment can include the bolt-on unit of the first embodiment, wherein the overhead gas from the existing demethanizer is at a pressure between about 250 psig to about 350 psig.

A third embodiment can include the bolt-on unit of the first or second embodiments, wherein the absorber and the reflux exchanger are fluidly coupled to a residue gas compressor and the demethanizer for 99% ethane recovery.

A fourth embodiment can include the bolt-on unit of any of the first to third embodiments, wherein a reduction device of the reflux liquid comprises a Joule-Thompson valve.

A fifth embodiment can include the bolt-on unit of any of the first to fourth embodiments, wherein, when ethane recovery of about 95% to 97% is the target, the refluxes are combined and fed to the demethanizer, eliminating the need for the absorber.

A sixth embodiment can include the bolt-on unit of any of the first to fifth embodiments, wherein, when ethane recovery of 97% to 99% is required, the demethanizer is modified with additional rectification trays, without the need for the absorber.

In a seventh embodiment a method may comprise passing an overhead vapor stream from a demethanizer to an absorber; contacting the overhead vapor stream with a cold lean residue gas to produce a liquid portion and a vapor portion within the absorber; passing the liquid portion back to the demethanizer as reflux; and passing the vapor portion to a subcooler, wherein the subcooler cools at least a first portion of the vapor portion to produce the cold lean residue gas.

An eighth embodiment can include the method of the seventh embodiment, further comprising: passing at least a second portion of the vapor portion to a second heat exchanger; and cooling at least a portion of a feed stream to the demethanizer with the second portion of the vapor portion in the second heat exchanger.

A ninth embodiment can include the method of the seventh or eighth embodiments, wherein passing the vapor portion to the subcooler comprises: passing the vapor portion to a first heat exchanger; cooling a compressed cooled residue gas using at least the first portion of the vapor portion in the first heat exchanger; compressing the first portion of the vapor portion downstream of the first heat exchanger to produce a compressed vapor portion; cooling the compressed vapor portion to produce the compressed cooled residue gas that passes to the first heat exchanger; and passing the compressed cooled residue gas to a pressure reduction device to produce the cold lean residue gas.

A tenth embodiment can include the method of the ninth embodiment, wherein the pressure reduction device comprises a hydraulic turbine or a Joule-Thompson valve.

An eleventh embodiment can include the method of any of the seventh to tenth embodiments, wherein the first portion of the vapor portion comprises between about 10% and about 30% of the vapor portion.

A twelfth embodiment can include the method of any of the ninth to eleventh embodiments, further comprising: separating a feed stream into a liquid portion and a feed gas vapor portion; cooling at least a first portion of the feed gas vapor portion in the subcooler using at least the first portion of the vapor portion; expanding at least a second portion of the feed gas vapor portion; and passing the expanded second portion of the feed gas vapor portion to the demethanizer.

In a thirteenth embodiment, a method may comprise passing an overhead vapor stream from a demethanizer to a first heat exchanger; cooling a compressed cooled residue gas using at least a first portion of the overhead vapor stream from the demethanizer in the first heat exchanger; compressing the first portion of the overhead vapor stream downstream of the first heat exchanger to produce a compressed vapor portion; cooling the compressed vapor portion to produce the compressed cooled residue gas that passes to the first heat exchanger; passing the compressed cooled residue gas to a pressure reduction device to produce a cold lean residue gas; and passing the cold lean residue gas to the demethanizer as reflux.

A fourteenth embodiment can include the method of the thirteenth embodiment, further comprising passing at least a second portion of the vapor portion to a second heat exchanger; and cooling at least a portion of a feed stream to the demethanizer with the second portion of the vapor portion in the second heat exchanger.

A fifteenth embodiment can include the method of the thirteenth or fourteenth embodiments, wherein the pressure reduction device comprises a hydraulic turbine or a Joule-Thompson valve.

A sixteenth embodiment can include the method of any of the thirteenth to fifteen embodiments, wherein the first portion of the overhead vapor stream comprises between about 10% and about 30% of the vapor portion.

In a seventeenth embodiment, a natural gas liquid plant bolt-on unit may comprise an absorber that condenses the ethane content from the overhead gas from a demethanizer using a cold lean residue gas to produce a liquid portion and a vapor portion, wherein the liquid portion is configured to provide to reflux to the demethanizer, and the vapor portion is configured to provide cooling of the reflux condenser and a subcooler; and a flow control valve, wherein the flow control valve is configured to pass about 10% to about 30% of the vapor portion to provide cooling to the recycle stream, and about 70% to 90% of the vapor portion to reflux cooling and reflux of the demethanizer.

In an eighteenth embodiment, a method may comprise passing an overhead vapor stream from a demethanizer to an absorber; producing a liquid portion and a vapor portion within the absorber; passing the liquid portion back to the demethanizer as reflux; and passing at least a first portion of the vapor portion to a subcooler, separating a feed stream into a liquid portion and a feed gas vapor portion; cooling at least a first portion of the feed gas vapor portion in the subcooler using at least the first portion of the vapor portion; expanding at least a second portion of the feed gas vapor portion; and passing the expanded second portion of the feed gas vapor portion to the demethanizer.

In a nineteenth embodiment, a method may comprise splitting an overhead vapor stream from a demethanizer into at least a first overhead portion and a second overhead portion; passing the first overhead portion to a first heat exchanger; cooling a compressed residue gas using at least the first overhead portion of the overhead vapor stream from the demethanizer in the first heat exchanger; compressing the first overhead portion downstream of the first heat exchanger to produce a compressed vapor portion; cooling the compressed vapor portion to produce at least a portion of the compressed cooled residue gas that passes to the first heat exchanger; passing the compressed cooled residue gas to a pressure reduction device to produce a cold lean residue gas; and passing the cold lean residue gas to the demethanizer as reflux.

A twentieth embodiment can include the method of the nineteenth embodiment, further comprising passing the second overhead portion to a second heat exchanger; and cooling at least a portion of a feed stream to the demethanizer with the second overhead portion in the second heat exchanger.

A twenty-first embodiment can include the method of the nineteenth or twentieth embodiments, wherein the pressure reduction device comprises a hydraulic turbine or a Joule-Thompson valve.

A twenty-second embodiment can include the method of any of the nineteenth or twenty-first embodiments, wherein the first portion of the overhead vapor stream comprises between about 10% and about 30% of the overhead vapor stream.

In a twenty-third embodiment, a natural gas liquid plant bolt-on unit may comprise a heat exchanger configured to receive a first portion of an overhead gas stream from a demethanizer, cool a compressed residue gas using at least the first portion of the overhead gas stream from the demethanizer in the heat exchanger, and pass the compressed cooled residue gas to the demethanizer as reflux; and a flow control valve, wherein the flow control valve is configured to pass about 10% to about 30% of the overhead gas stream to the heat exchanger.

A twenty-fourth embodiment can include the bolt-on unit of the twenty-third embodiment, wherein the flow control valve is further configured to pass about 70% to 90% of the overhead gas stream a subcooler to cool a first portion of an inlet gas stream.

A twenty-fifth embodiment can include the bolt-on unit of the twenty-third or twenty-fourth embodiments, further comprising a pressure reduction device configured to receive compressed cooled residue gas from the heat exchanger and reduce the pressure of the compressed cooled residue gas prior to passing the compressed cooled residue gas to the demethanizer as reflux.

While various embodiments in accordance with the principles disclosed herein have been shown and described above, modifications thereof may be made by one skilled in the art without departing from the spirit and the teachings of the disclosure. The embodiments described herein are representative only and are not intended to be limiting. Many variations, combinations, and modifications are possible and are within the scope of the disclosure. Alternative embodiments that result from combining, integrating, and/or omitting features of the embodiment(s) are also within the scope of the disclosure. Accordingly, the scope of protection is not limited by the description set out above, but is defined by the claims which follow that scope including all equivalents of the subject matter of the claims. Each and every claim is incorporated as further disclosure into the specification and the claims are embodiment(s) of the present invention(s). Furthermore, any advantages and features described above may relate to specific embodiments, but shall not limit the application of such issued claims to processes and structures accomplishing any or all of the above advantages or having any or all of the above features.

Additionally, the section headings used herein are provided for consistency with the suggestions under 37 C.F.R. 1.77 or to otherwise provide organizational cues. These headings shall not limit or characterize the invention(s) set out in any claims that may issue from this disclosure. Specifically and by way of example, although the headings might refer to a “Field,” the claims should not be limited by the language chosen under this heading to describe the so-called field. Further, a description of a technology in the “Background” is not to be construed as an admission that certain technology is prior art to any invention(s) in this disclosure. Neither is the “Summary” to be considered as a limiting characterization of the invention(s) set forth in issued claims. Furthermore, any reference in this disclosure to “invention” in the singular should not be used to argue that there is only a single point of novelty in this disclosure. Multiple inventions may be set forth according to the limitations of the multiple claims issuing from this disclosure, and such claims accordingly define the invention(s), and their equivalents, that are protected thereby. In all instances, the scope of the claims shall be considered on their own merits in light of this disclosure, but should not be constrained by the headings set forth herein.

Use of broader terms such as “comprises,” “includes,” and “having” should be understood to provide support for narrower terms such as “consisting of,” “consisting essentially of,” and “comprised substantially of.” Use of the terms “optionally,” “may,” “might,” “possibly,” and the like with respect to any element of an embodiment means that the element is not required, or alternatively, the element is required, both alternatives being within the scope of the embodiment(s). Also, references to examples are merely provided for illustrative purposes, and are not intended to be exclusive.

While several embodiments have been provided in the present disclosure, it should be understood that the disclosed systems and methods may be embodied in many other specific forms without departing from the spirit or scope of the present disclosure. The present examples are to be considered as illustrative and not restrictive, and the intention is not to be limited to the details given herein. For example, the various elements or components may be combined or integrated in another system or certain features may be omitted or not implemented.

Also, techniques, systems, subsystems, and methods described and illustrated in the various embodiments as discrete or separate may be combined or integrated with other systems, modules, techniques, or methods without departing from the scope of the present disclosure. Other items shown or discussed as directly coupled or communicating with each other may be indirectly coupled or communicating through some interface, device, or intermediate component, whether electrically, mechanically, or otherwise. Other examples of changes, substitutions, and alterations are ascertainable by one skilled in the art and could be made without departing from the spirit and scope disclosed herein.

Claims

1. A method comprising: passing an overhead vapor stream from a demethanizer to an absorber;contacting, within the absorber, the overhead vapor stream with a cold lean residue gas to produce a liquid portion and a vapor portion within the absorber;passing the liquid portion back to the demethanizer as a reflux; andpassing the vapor portion to a reflux exchanger, wherein the reflux exchanger cools at least a first portion of the vapor portion to produce the cold lean residue gas.

2. The method of claim 1, further comprising: passing at least a second portion of the vapor portion to a subcool exchanger;cooling, within the subcool exchanger, a portion of a feed stream;combining the portion of the feed stream with the second portion of the vapor portion; andpassing the combined portion of the feed stream and the vapor portion.

3. The method of claim 1, further comprising: compressing the first portion of the vapor portion downstream of the reflux exchanger to produce a compressed vapor portion.

4. The method of claim 3, further comprising: cooling the compressed vapor portion to produce a compressed cooled residue gas.

5. The method of claim 4, wherein the compressed vapor portion is cooled in the reflux exchanger.

6. The method of claim 5, wherein the compressed vapor portion is cooled in an air cooler prior to cooling in the reflux exchanger.

7. The method of claim 4, further comprising: passing the compressed cooled residue gas to a pressure reduction device to produce the cold lean residue gas.

8. The method of claim 7, wherein the pressure reduction device comprises a hydraulic turbine or a Joule-Thompson valve.

9. The method of claim 1, further comprising: separating a recycle portion from the first portion of the vapor portion downstream of the reflux exchanger.

10. The method of claim 9, further comprising: compressing the recycle portion to produce a compressed vapor portion.

11. The method of claim 10, further comprising: cooling the compressed vapor portion in an air cooler.

12. The method of claim 10, further comprising: separating a residue gas portion from the compressed vapor portion.

13. The method of claim 12, further comprising: cooling a remaining portion of the compressed vapor portion to produce a compressed cooled residue gas.

14. The method of claim 13, further comprising: passing the compressed cooled residue gas to a pressure reduction device to produce the cold lean residue gas.

15. The method of claim 14, wherein the pressure reduction device comprises a hydraulic turbine or a Joule-Thompson valve.

16. The method of claim 1, wherein the first portion of the vapor portion comprises between about 10% and about 30% of the vapor portion.

17. The method of claim 1, further comprising: separating a feed stream into a liquid portion and a feed gas vapor portion.

18. The method of claim 17, further comprising: cooling at least a first portion of the feed gas vapor portion in a subcool exchanger using at least the first portion of the vapor portion.

19. The method of claim 18, further comprising: expanding at least a second portion of the feed gas vapor portion.

20. The method of claim 19, further comprising: passing the expanded second portion of the feed gas vapor portion to the demethanizer.