Patent Application
20130035534
The present invention relates to a method and to an apparatus for separating hydrocarbons having two and/or more than two carbon atoms from a gas that contains methane, in particular for recovering NGLs from a pressurized natural gas, or for recovering LPG or NGLs from a refinery gas or to from gas of a different source.
Natural gas, as extracted from wells or taken from a gas pipeline, usually contains, apart from methane, hydrocarbons with two or more carbon atoms, hereafter indicated as C2+, in particular it contains ethane, propane and butane. C2+s are more valuable than methane, since they are a suitable starting material for a wide range of industrial chemical processes, for example olefin production; therefore, it is not advantageous to burn such hydrocarbons together with methane to obtain energy.
Similar considerations apply to the lightest fractions of crude oil atmospheric distillation, as well as to other refinery gas streams or to streams of gas obtained from a different source.
Therefore, it is a common practice to separate C2+ hydrocarbons from fuel methane, producing NGLs (Natural Gas Liquids, a mixture of ethane, propane, butane and C5+) or LPG (Liquefied Petroleum Gas, a mixture of propane and butane). This is made in treatment plants that are normally far from the gas fields, to which the plants are connected by gas pipelines that convey substantially raw natural gas, i.e. natural gas that has been subject to only rough physical treatments for separating foreign substances such as solid particles and water. The gas, in particular the natural gas, is normally available at the treatment plants at a pressure of tenths/hundreds of atmospheres.
With reference to attached
The above-described technique allows recovering C2+, in particular ethane, from gas 1, with a very high efficiency thanks to turbo expander 15, which is, however, a particularly critical component, and is affected by the quality of the fed gas. Raw gas 1, in particular a natural gas, generally contains moisture, which by cooling causes the production of particles of ice and of solid hydrates (water-hydrocarbons complexes) that cannot be tolerated by the turbo expander 15, which can be blocked and/or damaged in a very short time. Therefore, raw gas 1 is subject to expensive dehumidification treatments.
For example, the dehumidification can be carried out by causing gas 1 to flow through molecular sieve adsorption towers, which require a periodic regeneration and at least two alternated operation units 12′ and 12″, to ensure the continuity of the process; furthermore, means 18 for collecting and heating a stream of a regeneration gas 9 spilt from the dehumidified gas 2 are necessary, as well as a treatment unit, not shown, of the exhausted regeneration gas 10 is necessary. The dehydration section of the gas, which is necessary in order use the turbo expander 15, increases remarkably the preparation and operation costs of the prior art apparatus 100 for separating C2+ hydrocarbons, especially owing to the high energy demand of the regeneration section.
Furthermore, the turbo expander 15 as such is an expensive component, which causes operation, control and maintenance costs.
For the above reasons the separation of C2+, in particular of ethane can be not cost-effective with the known methods.
US 2005/0115273 A1 describes a combination of more fluid separation steps, typically from a gas extracted from a well, comprising at least one primary cooling apparatus for a gas with an outlet for a fluid in the liquid and/or solid state, and a separation container with a tubular vertical cross section connected to an outlet of the primary device by a tangential inlet duct. This combination, and specifically the primary device, however achieves an acceptable isentropic efficiency only if it operates with working parameters close to the design values. For treating a reasonably wide variety of flow rates, compatible with the possible variation which can occur during the operation, more devices in parallel are normally necessary.
FR 2 826 371 describes a process for pre-treating a natural gas as extracted containing acid compounds and water by means of partial condensation by cooling, dehydration by contact in two steps with a liquid stream containing hydrogen sulfide and final cooling for condensing, without water, the acid compounds. The pre-treatment has the object of avoiding the production of ice in cooling apparatus for separating the acid compounds, and to avoid the use of additives against the production of solid, such as methanol; the solution proposed is not suitable for most of the processes where a pressurized hydrocarbon gas containing C2+ is subject to expansion, owing to the use of hydrogen sulfide, especially when this acid compound is not present in the pressurized gas to treat, or it is present in an amount not important as the amounts indicated in the cited reference.
For separating methane from C2+ hydrocarbons, techniques are also known that use demethanization columns, associated with cooling systems. Even these techniques have preparation and operation costs which are often too high responsive to the recoverable amount of hydrocarbons with two or more carbon atoms.
It is therefore a feature of the present invention to provide a method for recovering hydrocarbons with two or more carbon atoms (C2+) starting from a wet fuel gas, where it is not necessary to dehydrate previously in an extensive way the wet fuel gas.
It is furthermore, a feature of the present invention to provide such a method that has preparation and operation costs lower than the methods of the prior art, achieving a same separation efficiency.
It is another particular feature of the present invention to provide such a method for recovering NGLs, or LPG, recovering propane and butane in a substantially quantitative way.
It is, furthermore, an a feature of the present invention to provide an apparatus for carrying out this method.
These and other objects are achieved by a method for separating at least one hydrocarbon with two or more carbon atoms in the liquid state starting from a substantially gaseous fluid containing methane, an amount of the at least one hydrocarbon with two or more carbon atoms and an amount of water higher than 3 parts per million by volume,
This way, it is possible to expand the substantially gaseous fluid, typically a natural gas coming from a natural gas field or from a gas transport pipeline, a refinery gas or another process gas that contains methane along with C2+ hydrocarbons, in order to cause an at least partial liquefaction or condensation of a considerable amount of hydrocarbons with two or more carbon atoms, recovering mixtures such as NGLs or LPG, since the first and/or second expansion equipment are capable of receiving and transferring fluids that contains large liquid amounts. Furthermore, the process for expansion and of liquefaction can be carried out even in the presence of a considerable amount of water, higher than 3 ppm, which alone or in combination with the hydrocarbons of the expanding fluid, can lead to the production of solid matter, such as ice and hydrocarbon hydrates, in an amount that would not be acceptable in a known expansion apparatus normally in use in the of expansion liquefaction systems of known type.
In particular, the use of a screw expansion device, of known type, as second expansion equipment, is advantageous due to the limited maintenance costs and also of acquisition typical of expanders of this kind.
The above-mentioned objects are also achieved by a device for separating in the liquid state an amount of at least one hydrocarbon with two or more carbon atoms starting from a substantially gaseous fluid containing methane, an amount of the at least one hydrocarbon with two or more carbon atoms and an amount of water higher than 3 parts per million by volume,
The device is arranged to receive the substantially gaseous fluid available at an extraction pressure set between 15 and 300 bar, in particular at a pressure set between 35 and 150 bar,
the device comprising:
Advantageously, the static expansion device comprises flow sections having a transversal size larger than a predetermined value, in particular larger than 4 mm, more in particular larger than 5 mm, much more in particular larger than 6 mm. This way, it is possible to execute the recovering of hydrocarbon liquid fractions, such as NGLs/LPG also in conditions of temperature and concentration of water that form solid aggregates of considerable size.
This allows the transit of small solid particles, in particular of particles of crystals that may form from water and by combination of the latter with the hydrocarbons of the expanding fluid, with substantially no risk of blocking and damaging the static device.
Advantageously, the substantially gaseous fluid has a residence time in static expansion device shorter than 5 milliseconds, in particular shorter than 3 milliseconds, more in particular shorter than 1 millisecond. This way, it is possible to limit the growth of the solid crystals that are formed during the expansion in the static device, in order not to achieve a size that is dangerous or that can block the device and the process for recovering the liquid fraction. In fact, limiting the residence time of the solid particles, for example due to the speed, which can be formed during the expansion in the static device, its growth is limited as well.
In an exemplary embodiment, the first expansion equipment and/or the second expansion equipment comprise furthermore:
The energy recovery device can be a compressor for compressing the substantially gaseous fluid after the liquefaction of the fraction of the at least one hydrocarbon with two or more carbon atoms.
Alternatively, or furthermore, the energy recovery device can be an electricity generator.
In particular, also in the presence of solid and liquid in the gas during the expansion, the screw expansion device that can be used as second expansion equipment may have a speed about 1500 RPM, which is compatible with the direct coupling with an electric generator connected to the network, with a mechanical simplification of the device. Therefore, advantageously, the second expansion equipment comprises a screw expansion device, and said to mechanical connection means is a direct connection means that is arranged to cause a rotation of a rotor of the electric generator at the same speed of the rotor of said screw expansion device.
In an exemplary embodiment, said expansion device comprises
a tubular inlet portion which is adapted to receive an at least partially gaseous fluid at a predetermined inlet pressure, the tubular inlet portion having an inlet port, an inlet surface consisting of the inner surface of the tubular inlet portion, a longitudinal axis and a generally decreasing cross sectional area, starting from the inlet port;
a tubular outlet portion for the at least partially gaseous fluid;
a tubular throat portion between the tubular inlet portion and the tubular outlet portion, such that the tubular throat portion forms a passageway for an at least partially gaseous fluid;
a closing element, which is arranged in the throat portion, in order to cause an expansion with pressure drop down to a predetermined discharge pressure, a cooling and a partial liquefaction of the at least partially gaseous fluid;
where in the inlet portion a means is provided for directing fluid at least partially in the gaseous state according to a flow direction that is generally at an angle with respect to the longitudinal axis, in order to reduce the friction of the at least partially gaseous fluid when flowing through the device, in particular through the throat portion at the closing element.
In an exemplary embodiment, the means for directing the at least partially gaseous fluid comprises channels arranged along the inner surface of the inlet portion.
In particular, the inlet portion comprises a central portion that has a central surface such that an annular passage is defined, where the channels are defined by a plurality of baffles that are arranged according to the flow direction along the annular chamber.
In particular, the means for directing that are arranged in the inlet portion are adapted to impart to the fluid a swirling movement such that a centrifugal force acts on the at least partially gaseous fluid and a transformation occurs of a pressure energy into a kinetic energy that is associated with the swirling movement, and such that this centrifugal force assists a separation between to the gas phase and the progressively forming liquid phase.
Such a static expansion device, in addition to allow/assist the expansion of a large amount of liquid and/or of solid that can form starting from water and/or from some hydrocarbons of the fluid, provides a substantially isentropic transformation, i.e. a transformation at a high rate of isentropicity, which differs from a reversible isentropic transformation between the inlet pressure and the discharge pressure less than static expansion devices of known type, i.e. a transformation more similar to that of a dynamic expansion device, increasing the cooling effect and then the amount of liquid recovered under same inlet/outlet conditions and features of the gas that is expanded.
Advantageously, the central surface comprises a surface of a central element having the shape of a solid of revolution, in particular of an ogive-shaped element fixedly arranged in the inlet portion, the ogive-shaped element having an axis that preferably coincides with the longitudinal axis of the inlet portion.
In particular, the closing element is a substantially cylindrical hollow body coaxially connected to one end of the central element opposite to the inlet port of the inlet portion, the cylindrical hollow body having a plurality of holes formed between an outer cylindrical surface and an inner cylindrical surface, at least one part of the holes arranged proximate to channels of the inlet portion, such that a portion of the at least partially gaseous fluid that leaves one of the channels enters and flows through a respective hole of the closing element gradually achieving a swirling direction that is maintained within an inner recess of the closing element and/or within the outlet portion of the expansion device.
This way, the central element for directing the fluid in the inlet portion, in particular in case of helical channels, is adapted to create a swirling movement of the fluid, such that a centrifugal force acts on the fluid and, while the gas flows through a progressively decreasing passage area a transformation occurs of a pressure energy into a kinetic energy that is associated with the swirling movement, and at the same time the centrifugal separation of the resulting liquid phase from the gas phase is enhanced.
In particular, each baffle is integral with a respective connection surface selected between the central surface and the peripheral surface of the annular to chamber.
Preferably, all the baffles are integral to a same connection surface, selected between the central surface and the peripheral surface of the annular chamber.
Preferably, the channels have a helical profile, i.e. they are arranged along respective adjacent spirals on the connection surface of the baffles. This way, the at least partially gaseous fluid follows a swirling movement which has the above described advantages.
In particular, each baffle is housed in a respective seat that is made on a surface of the chamber opposite to the respective connection surface, such that a seal is provided between adjacent channels of the plurality of channels.
Advantageously, the substantially cylindrical closing element is slidingly arranged within a recess of the central element, such that, as a consequence of a relative sliding movement of the closing element and of the central element, a change is produced of the width of the throat portion that is defined between the closing element and the peripheral surface, and a change is produced of the pressure drop of the at least partially gaseous fluid.
The invention will be made clearer with the description of an exemplary embodiment thereof, exemplifying but not limitative, with reference to the attached drawings, in which the same reference characters designate the same or similar parts, throughout the figures of which:
FIGS. 13′,13″ are exploded views of exemplary embodiments of the expansion device according to the invention, in particular FIG. 13′ relates to the exemplary embodiment of
With reference to
Stream 3 is supplied to an expansion device 20, comprising a first expansion equipment 19, that is arranged to receive substantially gaseous fluid 3 and to cause it to follow a first expansion, such that it turns into a fluid 4 that is at least partially in the gaseous state at pressure P2 less than pressure P1 of stream 3 as it entered first expansion equipment 19,24. When turning from pressure P1 to pressure P2 the fluid is subject to a cooling from temperature T1 to temperature T2 larger than the solid formation temperature, where solids like ice and hydrates can be formed starting from water contained in substantially gaseous fluid 1 and then also in substantially gaseous fluid 3.
Stream 4 is supplied to a first separation chamber 16 where it is separated into a liquid fraction 5, preferably collected in first separation chamber 16, and a gas fraction 6, according to mutual ratios that depend on the pressure drop and on the temperature decrease that occurs in first expansion equipment 19,24, i.e. at values P2,T2 of pressure and temperature reached at the exit of first expansion equipment 19,24.
In parallel to first expansion equipment 19,24 a bypass line is provided along which a Joule-Thomson expansion valve is arranged 15, which is activated by valves during a start-up phase of treatment unit 200,300,400 or in case of maintenance of first expansion equipment 19,24.
Along the flow and expansion passage of the fluid in device 20, through separation chamber 16, a second expansion equipment 25,30 is arranged for a further expansion of gas 6 coming from separation chamber 16, already expanded by first expansion equipment 19,24, even in the presence of considerable amount of solid, that can be formed owing to the concentration of water in the gas 3 higher than 3 ppm. Passing through second expansion equipment 25,30 the gas turns into a fluid 7 that is at least partially in the gaseous state at pressure P3 less than pressure P2 of stream 6 as it entered second expansion equipment 25,30. When turning from pressure P2 to pressure P3 the fluid is subject to a cooling from temperature T2 to temperature T3 less than the solid formation temperature.
Stream 7 is supplied to a second separation chamber 16′ where a liquid fraction 8 is separated, preferably collected in second separation chamber 16′, and a substantially gaseous fraction 9, according to mutual ratios that depend on the pressure drop and on the temperature decrease that occurs in second expansion equipment 25,30, i.e. at values P3,T3 of pressure and temperature reached at the exit of second expansion equipment 25,30.
Liquid fractions 5 and 8 are drawn through respective pumps 17,17′, or equivalent propelling means, and sent to respective storage or use devices, not depicted. Liquid fractions 5 and 8 can be used as cooling fluid in exchanger 14″ where a preliminary cooling is achieved of portion 2″ of the stream of substantially gaseous fluid 2.
Gas fraction 9 mainly comprises methane and residues of hydrocarbons with two or more carbon atoms, which are normally destined to combustion along with methane. Their separation would require in fact the use of turbo expander expansion apparatus that would be more expensive than the turbo expander apparatus used in the device according to the invention, and that would require, furthermore, as described, accurate and expensive gas dehydration operations, in most of the cases not justifiable versus the actual residual benefits that could derive from recovering the C2+ fraction.
Substantially gaseous stream 9, substantially still at temperature T3 obtained by the Joule-Thomson effect in device 20, is used as cooling fluid in exchanger 14′, where the preliminary cooling is achieved of portion 2′ of stream 2. Then, gas fraction 6 reaches in a compressor 28 a compression at a pressure P4, such that an effective transport of gas fraction 6 can be achieved from apparatus 200, 300, 400 through a natural gas distribution pipeline, up to a storage and/or use location, not shown.
In parallel to second expansion equipment 25,30 a bypass line is provided along which a Joule-Thomson expansion valve 15′ is arranged, which is activated by valves during a start-up phase of treatment unit 200,300,400 or in case of maintenance of second expansion equipment 25,30.
In the exemplary embodiment shown in
Screw expansion device 25 and static expansion device 30, of the type described hereinafter, in particular, with reference to
In an apparatus 500 or 700, a single energy recovery device is provided comprising an electric generator 29, for recovering energy from the expansion of fluid 3 in the form of an electric power W whereas in an apparatus 600 both a compressor 28 for compressing gas stream 9 that leaves separator 16, and an electric generator 29 are provided. In particular, apparatus 500 of
With reference to
Stream 3 is supplied to an expansion device 20, comprising a first expansion equipment 19, that is arranged to receive substantially gaseous fluid 3 and to cause it to follow a first expansion, such that it turns into a fluid 4 that is at least partially in the gaseous state at pressure P2 less than pressure P1 of stream 3 as it entered first expansion equipment 19,24. When turning from pressure P1 to pressure P2 the fluid is subject to a cooling from temperature T1 to temperature T2 that is higher than the solid formation temperature, at which ice and hydrates can form starting from the water contained in substantially gaseous fluid 1, and then also in substantially gaseous fluid 3.
In parallel to first expansion equipment 19,24 a bypass line is provided along which a Joule-Thomson expansion valve is arranged 15, which is activated by valves during the start-up step of treatment unit 200,300,400, or in case of maintenance of first expansion equipment 19,24.
Downstream of first expansion equipment 19,24, along the path where the fluid of device 20 flows and expands, a second expansion equipment 25,30 is arranged for a further expansion of gas 4 that has been expanded by first expansion equipment 19,24, also in the presence of a considerable amount of solid, such as the solid that is formed owing to concentration of water in gas 3 higher than 3 ppm. When crossing second expansion equipment 25,30, it turns into a fluid 7 that is at least partially in the gaseous state at pressure P3, which is less than pressure P2 of stream 4 that enters second expansion equipment 25,30. When turning from pressure P2 at pressure P3 the fluid is subject to a cooling from temperature T2 to temperature T3 less than the formation temperature of the solid.
Stream 7 is supplied to a separation chamber 16′ where it is separated into a liquid fraction 8, preferably collected in separation chamber 16′, and a to substantially gaseous fraction 9, according to mutual ratios that depend on the pressure drop and on the temperature decrease that occurs in device 20, i.e. in first expansion equipment 19,24 of in second expansion equipment 25,30.
Liquid fraction 8 is drawn through pump 17, or means equivalent and that is arranged to storage or use, not depicted. Liquid fraction 8 can be used as cooling fluid in exchanger 14″ where preliminary cooling occurs of portion 2″ of substantially gaseous fluid stream 2.
Gas fraction 9 mainly comprises methane and residues of hydrocarbons with two or more carbon atoms, which are normally destined to combustion along with methane. It is substantially still at temperature T3, which is reached by Joule-Thomson effect in device 20, and is advantageously used as cooling fluid in exchanger 14′ where a preliminary cooling occurs of portion 2′ of stream 2.
Device 20 comprises, in parallel to first expansion equipment 19,24 and to second expansion equipment 25,30, a bypass line along which a Joule-Thomson expansion valve 15′ is arranged, which is activated by valves during start-up of treatment unit 500,600,700 or in case of maintenance of second expansion equipment 25,30.
In the exemplary embodiment shown in
In the exemplary embodiment of
The description is referred to a method and to an apparatus for C2+ recovery from a wet natural gas, but can also refer to other gas that contains methane and hydrocarbons with two or more carbon atoms, for example a gas associated with a natural gas field or a refinery gas, for example a gas coming from crude oil atmospheric distillation or gas coming from a different source containing C2+.
In apparatus 500 and apparatus 700, a single energy recovery device is provided comprising an electric generator 29, for recovering energy from the expansion of fluid 3 as an electric power W, whereas in apparatus 600 both a compressor 28 for compressing gas stream 9 exiting from separation chamber 16, and an electric generator 29, are provided. In particular, apparatus 500 of
In an exemplary embodiment, not shown, a device for separating by means of liquefaction at least one hydrocarbon with two or more carbon atoms comprises a plurality of first expansion equipment arranged parallel to each other and/or a plurality of apparatus for second expansion equipment that is arranged parallel to each other.
Surface 42 comprises an ogive-shaped element 40, which is shown more in detail in
Baffles 41 define a plurality of channels 46 (
Downstream of inlet portion 31 there is a tubular throat portion 65, where closing element 60 is arranged movable within said throat portion 65 such that, while crossing throat portion 65, at least partially gaseous fluid stream 3 has a pressure drop, turning into an at least partially gaseous fluid stream 3′ at a pressure P2 lower than inlet pressure P1.
Baffles 41, whose shape collaborates to define the decrease of passageway 33, in particular within throat portion 65, and therefore the pressure drop, impart to the flow a centrifugal component, and a substantially helical advancing movement through a throat 65′ left free from closing element 60.
Inlet pressure P1, at which stream 3 is supplied, is higher than the pressure at which stream 3′ leaves throat portion 65, a partial pressure recovery occurring at the expenses of the kinetic energy the fluid has in an outlet zone 66. The pressure drop ΔP=P2−P1 normally depends upon pressure P1, at which it stream 3 is available, and upon stream 3 flow rate. In case of a stream of a gas in which no liquid phase is present, such a pressure drop may cause a partial liquefaction of the gas, therefore stream 3 may turn into an at least two-phase mixture where a liquid phase is present. More in detail, pressure drop ΔP and a subsequent temperature decrease ΔT may, according to Joule-Thomson effect, bring the gas to pressure and temperature conditions where a liquid-vapour system is thermodynamically stable, such that stream 3′ downstream of throat portion 65, i.e. downstream of closing element 60, is a multiphase stream where at least one phase is a liquid phase, even if a liquid phase is missing in stream 3. Downstream of closing element 60 and of throat portion 65 a tubular expansion portion 66 is provided for stream 3′ that turns into stream 4.
In an exemplary embodiment, throat section 65′ doesn't close for any position of closing element 60, in order to allow in any case the passage of possible solid bodies.
Due to a relative sliding movement of closing element 60 and of central element 40 a change occurs in the width of throat portion 65, which is defined between closing element 60 and peripheral surface 92, in particular a change of the cross sectional area of multiple throat defined by holes 61, which have respective outlet ports cut by closing element 60. This way, it is possible to adjust pressure drop ΔP=P2−P1 and/or the flow rate of stream 3-3′.
FIG. 13′ is an exploded view of device 30 according to the exemplary embodiment shown in
FIG. 13″ is an exploded view similar to the view of FIG. 13′, where another exemplary embodiment of device 30 is shown, where baffles 91,71 that define the helical channels of inlet portion 31 are integral to the peripheral surface formed by inner surface 92 of the body of device 30′ and by inner surface 72 of ring element 70. The detail of the exemplary embodiments of body 30′, of ogive-shaped element 80 and of ring element 70, corresponding to the exemplary embodiment of the device of in FIG. 13″, is shown, in the order, in
In particular, in
The details that are described along with the exemplary embodiment of FIG. 13″ are shown in
In the represented exemplary embodiments, all baffles 41,71,91 are integral to a same central or peripheral connection surface 42,72,92, however an exemplary embodiment may be provided in which some baffles are integral to central surface 42 and other baffles are integral to a peripheral surface 72,92.
The foregoing description of exemplary embodiments of the method and of the apparatus according to the invention, and of the use thereof, will so fully reveal the invention according to the conceptual point of view, so that others, by applying current knowledge, will be able to modify and/or adapt for various applications such exemplary embodiments without further research and without parting from the invention, and it is therefore to be understood that such adaptations and modifications will have to be considered as equivalent to the specific embodiment. The means and the materials to perform the different functions described herein could have a different nature without, for this reason, departing from the field of the invention. It is to be understood that the phraseology or terminology that is employed herein is for the purpose of description and not of limitation.
| Number | Date | Country | Kind |
|---|---|---|---|
| PI2010A000041 | Mar 2010 | IT | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/IB2011/000682 | 3/30/2011 | WO | 00 | 9/29/2012 |
