• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention describes a liquid-liquid extraction column with perforated plates (Po) and weirs, the plates being furthermore equipped with an additional friction element (Pad) which makes it possible to increase the thickness of the coalesced layer and to guarantee a countercurrent flow of the continuous and dispersed phases. The extraction column is used, for example, for extracting sulfur compounds from a hydrocarbon phase with an aqueous solution of sodium hydroxide.
    公开号:CH707291B1
    申请号:CH01914/13
    申请日:2013-11-15
    公开日:2017-06-30
    发明作者:Leinekugel-Le Cocq Damien；Augier Frédéric
    申请人:Ifp Energies Now；
    IPC主号:
    专利说明:

    Description
    FIELD OF THE INVENTION [0001] The invention relates to the field of liquid-liquid extraction or solvent extraction operations, bringing a hydrocarbon phase into contact with a phase that is partially immiscible with the hydrocarbon feedstock and containing a fraction of water. .
    A particular case is the extraction of sulfur compounds from a hydrocarbon phase with an aqueous solution of sodium hydroxide (concentrated from 10% to 20% by weight relative to the total solution), the hydrocarbon phase then being the dispersed phase, and the aqueous sodium hydroxide solution the continuous phase.
    Examination of the Prior Art [0003] The principle of solvent extraction between two partially immiscible liquid phases has been known for several decades. If a raffinate phase containing the solute is brought into contact with an extracted phase containing no (or little) phase, a transfer of the solute takes place from one phase to the other until a thermodynamic equilibrium is reached between the two phases.
    The phenomenon is greatly facilitated if, at thermodynamic equilibrium, the concentration of solute in the extracted phase is greater than that in the raffinate phase. The concentration ratio between the two phases at equilibrium is called the partition coefficient.
    A usual implementation of liquid-liquid extraction is to bring the two liquids in contact against the current, that is to say in opposite flow directions. In case of extraction in a column positioned vertically, it is called a light phase and a heavy phase.
    A very common case is that of systems composed of an organic or hydrocarbon phase and an aqueous phase. In this case, the aqueous phase is very often the heavy phase. In the liquid-liquid extraction, it is also necessary to distinguish the continuous phase and the dispersed phase.
    The continuous phase follows a flow as close as possible to the piston flow, that is to say without retro mixture.
    The dispersed phase follows a flow generally against the current of that of the continuous phase and passes through a system of perforated trays that allows the formation of droplets, droplets that coalesce to form a coalesced layer located under each perforated tray when the phase dispersed is the light phase (above each plateau when the dispersed phase is the heavy phase).
    The exchanges of material between continuous phase and dispersed phase are essentially between the droplets of the dispersed phase and the continuous phase flowing over each plate.
    The implementation against the current makes it possible to constitute several successive theoretical stages in the column, and thus to achieve an extraction efficiency much greater than that obtained with a single stage corresponding to the thermodynamic equilibrium.
    A more precise description of liquid-liquid extraction operations is provided in numerous dedicated works, including Handbook of Solvent Extraction Lo, Baird & Hanson, Krieger Publishing Company, Malabar, 1991, or Transport Phenomena in Liquid Extraction from Laddha & Degaleesan, Tata McGraw-Hill Publishing Co Ltd, 1976.
    The concepts of theoretical stages are described in particular, which is an important point to understand the interest of the invention.
    In an extraction column trays and weirs, the dispersed phase must form a coalesced layer under the plate when the dispersed phase is the light phase, or above the plateau when the dispersed phase is the heavy phase. The thickness of this coalesced layer must be such that it ensures that the plate is always in contact with said coalesced phase. A break in this coalesced phase, even on only a part of the plateau can cause a significant deterioration of the performance of the column. Indeed, in the case where the coalesced layer does not cover the entire surface of the perforated plate, there is flow of the continuous phase through the plate, thus inducing lower than expected extraction performance. This is the phenomenon called "weeping".
    The rupture of the coalesced layer may occur for various reasons, for example following a plateau flatness problem, or disturbances of the interface between the coalesced layer and the continuous phase.
    The thickness of the coalesced layer is determined by the pressure losses associated with the flow of the two phases. The various contributions are detailed on page 15-36 of the Perry's Chemical Engineers Handbook, 7th ed. Mc Graw-Hill, 1999. The contribution related to the continuous phase is related to pressure losses in the weir. The dispersed phase contributes in two ways: - by its flow through the perforations of the plate, - by the effects related to the interfacial tension put into play during the formation of drops.
    Each of these contributions is inversely proportional to the difference in densities of the two liquid phases. Thus, the higher the density difference, the less the coalesced layer is thick.
    In addition, the term related to the pressure drop due to the flow through the perforations of the plate is generally predominant. But this term is proportional to the density of the dispersed phase. Thus, the more the dispersed phase is light, the less coalesced layer is thick.
    When the ratio between the density of the dispersed phase and the difference in density of the liquid phases is too low, it is necessary to use a speed at the crossing of the orifices of the very high dispersed phase to ensure a coalesced layer thickness. minimal. However, a high speed at the crossing of the orifices results in a very wide distribution of drop size, with the formation of fine droplets that can be driven by the continuous phase in the weir, thus inducing lower than expected extraction performance.
    It is generally recommended to operate the liquid-liquid extraction column with an optimum speed through the orifices, (said optimum value depending on the liquid-liquid system considered) while having a coalesced layer thickness greater than a low limit of between 30 mm and 70 mm.
    The speed at the crossing of optimal orifices can be calculated according to different methods, described in the Handbook of Solvent Extraction, already mentioned above. The desired flow regime is that in which the phase to be dispersed leaves the hole in the form of a continuous stream of maximum size.
    The breaking of this jet then generates droplets of small sizes, ideal for transfer between phases. The optimum speed range at the ports is typically between 0.15 and 0.3 m / s, according to Handbook of Solvent Extraction.
    However, it is not possible to simultaneously meet these two criteria when the difference in density between the two phases is high (greater than 300 kg / m3), and that the light phase has a low density (less than 700 kg). / m3).
    In case of a large difference in densities between phases, compliance with a minimum thickness of coalesced layer implies a speed at the through of the orifices which may be higher than the recommended speed to generate a maximum size jet output of holes.
    As a result, the droplets formed may be of nonhomogeneous sizes, which is detrimental to the transfer and the hydrodynamics. In fact, the fine droplets may be entrained in the weirs, which can degrade the performance of the process.
    The column according to the present invention is a liquid-liquid extraction column with trays specifically adapted to the system having a high density difference between the two liquid phases, and whose light phase has a low density, so as to guarantee the existence of a coalesced layer above or below each plateau.
    The existence of this coalesced layer is essential to prevent the phenomenon of pleurage and allow flow against the current of the continuous phase and the dispersed phase.
    The present invention therefore describes a liquid-liquid extraction column equipped with specific trays that provide sufficient pressure drop across said trays, even when the density ratio of the dispersed phase on the mass difference volume of the two phases (dispersed and continuous) is low.
    This density ratio can in particular become very low when the difference in density between heavy phase and light phase becomes significant (for example greater than 300 kg / m3).
    In the prior art, US Pat. No. 2,872,295 describes a multi-stage column comprising trays which consist of a set of two trays having different porosities. These trays are connected in such a way that a liquid layer can be established in the space between the two trays.
    There may also be mentioned US 2,794,711 which teaches a device allowing the intimate contact of two liquids by means of contact trays and dispersion baffles. No information on a possible difference in the degree of opening of the trays is provided in this document.
    Brief description of figures [0031]
    Fig. 1 shows a liquid-liquid extraction column with trays and weirs according to the prior art.
    Fig. 2 shows the liquid-liquid extraction column according to the present invention in which each plate is equipped with an additional friction element which is here a plateau with a porosity strictly less than the porosity of the open plate.
    Fig. 3 shows a top view of a plate according to the invention equipped with an additional friction element which is a plate of strictly lower porosity with its orifices offset from those of the open plate.
    Brief Description of the Invention [0032] The present invention can be defined as a countercurrent liquid-liquid extraction column with perforated weir trays contacting a light dispersed phase and a heavy continuous phase, the solute being transferred. from the dispersed phase to the continuous phase, said column being provided with open trays with a degree of perforation of between 2% and 6% and each open tray being completed by an additional friction element of porosity strictly smaller than that of the open tray, each friction element being placed below each open tray at a distance between 0.5 cm and 5 cm below said tray.
    When the dispersed phase is the heavy phase and the continuous phase is the light phase, the definition of the extraction column according to the present invention becomes:
    Countercurrent liquid-liquid extraction column with perforated perforated trays, contacting a heavy dispersed phase and a continuous light phase, the solute being transferred from the dispersed phase to the continuous phase, said column being provided with open trays with a degree of perforation of between 2% and 6%, supplemented by additional friction elements of porosity strictly less than that of the open plate, each friction element being placed above each open plate at a distance of between 0.5 cm and 5 cm above the tray.
    The porosity expressed in% represents the empty fraction of the plate relative to the free section of the column.
    According to a first variant of the present invention, the additional friction elements are perforated plates located below (or above if the dispersed phase is the heavy phase) of each open plate having a porosity equal to p times that of the open plate p being between 0.6 and 0.9.
    According to a preferred feature of the present invention, the additional friction elements when they are trays have their orifices offset from those of the open plate to which it is attached.
    According to another variant of the present invention, the additional friction elements consist of one or more layers of a woven fiber material.
    According to a preferred feature of the present invention, the weirs of each tray have a passage section of between 6% and 20% of the free section of the column.
    According to another preferred feature of the present invention, the number of trays of the extraction column according to the present invention is between 4 and 25, and preferably between 6 and 20.
    The extraction column according to the present invention is particularly applicable to the extraction of sulfur compounds from a hydrocarbon phase by an aqueous sodium hydroxide solution representing from 10% to 20% by weight, the hydrocarbon phase being the phase dispersed.
    Finally, the extraction column according to the present invention is particularly applicable to the case where the difference in density between the heavy phase and the light phase is greater than 300 kg / m3 and the density of the light phase is less than 750 kg / m3.
    DETAILED DESCRIPTION OF THE INVENTION [0042] The invention relates to a countercurrent liquid-liquid extraction column with perforated trays and weirs, implementing a heavy phase and a light phase between which a solute is exchanged. the difference in density between the two liquids being high (greater than 300 kg / m3), and the density of the light phase being low (less than 750 kg / m3).
    The light phase may be as the case the continuous phase or the dispersed phase.
    In the rest of the text, for clarity, we will take the case of a dispersed light phase, but the column according to the invention is equally applicable to the case of a heavy light phase.
    The essential difference between the two cases is that, in the case of a light dispersed phase, the coalescence layer is below the plateau, and in the case of a heavy dispersed phase, it is found above said plateau.
    The object of the invention is to ensure proper operation of the extraction column by ensuring a minimum coalesced layer thickness (that is to say greater than 7 cm), and a speed at the crossing orifices of each optimum plateau to generate drops having a very narrow size distribution.
    The invention cleverly combines a so-called "open" perforated plate (Po) having a large perforated surface, so as to guarantee an optimum through-hole speed corresponding to a continuous jet of dispersed phase of maximum size. at the outlet of the orifice, and a piece of equipment that we will later call "additional friction element" (Pad) making it possible to ensure a coalesced layer thickness greater than 7 cm. The friction element (Pad) is located within the coalesced layer of dispersed phase, and at a distance of between 0.5 cm and 5 cm from the open plate with which it is associated.
    It generates losses on the dispersed phase such that the coalesced layer thickness is greater than 7 cm.
    According to a first variant of the column according to the invention, the friction element (Pad) for generating the additional pressure drop is a second perforated plate.
    If the dispersed phase is the light phase, the additional friction element (Pad) is located under the open perforated tray (Po).
    If the dispersed phase is the heavy phase, the additional friction element (Pad) is located above the open perforated tray (Po).
    The degree of perforation of the additional friction element (Pad) is strictly less than that of the "open" perforated plate (Po) in a ratio p between 0.6 and 0.9, and preferably between 0. , 6 and 0.8.
    The degree of perforation of the open tray is between 2% and 6% based on the empty column section. To calculate the degree of perforation of the friction element, the ratio p is then applied to the degree of perforation of the open plate.
    The perforations of the friction element (Pad) are positioned so as not to be in the same vertical axis as the perforations of the open perforated tray (Po), as shown in FIG. 3.
    According to a preferred variant of the present invention, the perforations of the friction element (Pad) may be offset so as to be in opposition to the perforations of the open plate (Po), as shown in FIG. fig. 3. It is clear that this offset arrangement of the friction element relative to the open plate maximizes the pressure drop caused by said element.
    According to a second variant of the method according to the invention, the friction element (Pad) for generating the additional pressure drop is a set of woven fibers. This friction element thus facilitates the coalescence of the dispersed phase and makes it possible to maintain the thickness of the coalesced layer (Ch) in the desired range.
    More specifically, FIG. 1 according to the prior art describes a liquid-liquid extraction column supplied with a heavy phase by line 2, and in a light phase via line 3.
    The heavy phase which is the continuous phase comes out at the bottom of the column by the pipe 5, and the light phase which is the dispersed phase comes out at the top through the pipe 4.
    The column is equipped with 8 open type weir trays numbered P1 to P8. Each open tray is composed of a perforated plate (6) and a weir (7).
    The loss of charge generated at the traversing trays induces the presence of a coalesced dispersed phase layer (8) under each tray.
    The cross section and the shape of the weir closed plateau can be constant over its entire length, or variables as shown in FIG. 1 by the elements of different sections (10) and (12).
    FIG. 2 according to the invention shows more precisely the association of a plate noted Po with its friction element which is here a plateau noted Pad. The layer coalesced under the plate is noted Ch.
    D denotes the weir whose section is between 6% and 20% of the free section of the column.
    FIG. 3 according to the invention shows in plan view an open plate associated with its additional perforated plate located below (or above if the dispersed phase is the heavy phase), the additional perforated plate having a porosity equal to p times that of the open plate, p being between 0.6 and 0.9. We show in fig. 3 the offset between the openings (To) of the open platform and those (Tad) of the closed plateau located below.
    The section (D) of the weir representing approximately 8% of the free section of the column is also shown.
    Comparative Example According to the Invention [0066] The following comparative example is obtained by simulation.
    The feedstock to be treated is a LPG (liquefied petroleum gas) containing 100 ppm of methanethiol.
    The solvent used to extract the methanethiol is a 20% sodium hydroxide solution.
    The dispersed phase is the hydrocarbon phase. The continuous phase is the soda solution.
    The LPG and soda flow rates are 165 and 4.3 m3 / h respectively.
    The extraction is carried out at 30 ° C. and under 10 bars absolute.
    Three separate devices are used to perform the extraction. 1) The device 1 said "open trays" is according to the prior art.
    It consists of an extraction column equipped with 15 perforated trays with spillways, 1 m apart, and 2.9 m in diameter. The perforations are 5 mm in diameter and the perforated surface is equal to 2.9% of the
    权利要求:
    Claims (7)
    [1]
    column section, so as to have a speed through the orifices of 0.24 m / s, as recommended in the prior art. Weirs have an area equal to 7.3% of the column section. The layer thickness coalesced in the tray is then 1 cm. 2) The device 2, still according to the prior art, is called "closed trays". It is in all respects similar to the device 1, but the perforated surface is equal to 0.7% of the column section. The speed through the orifices is then 1.01 m / s. The layer thickness coalesced under the plate is then 10 cm. 3) The device 3 is according to the invention. It consists of an extraction column equipped with 15 open-type trays, such as those fitted to the device 1, each tray according to the device 1 being associated with a closed tray according to the device 2, the additional closed plate being located at below the open tray. The open tray assembly (Po) / closed tray (Pad) forms the tray according to the invention. Each additional closed tray is located under an open tray, at a distance of 0.8 cm from the latter. The perforations of each additional closed plate are positioned so as not to be in line with the performances of the open plate situated just above. The open trays are 1 m apart. The speed through the orifices is 0.24 cm / s. The thickness of the coalesced layer resulting from the tray according to the invention is 10 cm. The comparison between the three devices can be summarized as follows: 1) The device consisting of open trays does not ensure sufficient coalesced layer thickness over the entire section of the column to avoid the problems of retro mixture of soda which is the continuous phase. The small thickness of the coalesced layer of the hydrocarbon phase allows a fraction of the continuous phase of soda to pass through the perforated plate, causing the phenomenon of pleurage and discarding the flow of the desired piston regime. This device therefore no longer makes it possible to guarantee a suitable flow against the current. As a result, the set of open trays behaves as a single theoretical stage. 2) The closed tray device provides a large coalesced layer thickness, but due to the diameter of the orifices, the velocity through the orifices is so high that fine droplets of dispersed phase are formed. These fine droplets of dispersed phase pose problems of coalescence under the plate, which induces a retro mixture of soda, as well as a problem of retro mixture of the hydrocarbon phase due to the entrainment of the finest droplets in the weirs by the continuous phase of soda. This device therefore no longer makes it possible to guarantee a suitable flow against the current. As a result, the set of closed trays behaves as a single theoretical stage. 3) Finally, the device according to the invention ensures a good flow against the current, maintaining a large coalesced layer thickness and generating a narrow drop size distribution. The trays then have an efficiency of 18.7%. The device therefore has a theoretical number of stages equivalent to 2.8. claims
    1. Countercurrent liquid-liquid extraction column with perforated perforated trays (p1-p8) contacting a light dispersed phase and a heavy continuous phase, the solute being transferred from the dispersed phase to the continuous phase, characterized in that each perforated weir tray is provided with an open tray with a degree of perforation of between 2% and 6% (Po) supplemented by an additional friction element (Pad) with a porosity strictly smaller than that of the open tray (Po) ), each additional friction element (Pad) being a perforated tray placed beneath each open tray (Po) at a distance of between 0.5 cm and 5 cm below said open tray (Po), and the factor reducing the porosity of each additional friction element (Pad) being between 0.6 and 0.9 relative to the porosity of an open plate (Po).
    [2]
    2. Counter-current liquid-liquid extraction column with perforated perforated trays (p1-p8) contacting a heavy dispersed phase and a light continuous phase, the solute being transferred from the dispersed phase to the continuous phase, characterized in that each perforated perforated tray is provided with an open tray (Po) with a degree of perforation of between 2% and 6% supplemented by an additional friction element (Pad) of porosity strictly smaller than that of the open tray (Po ), each additional friction element (Pad) being placed above each open plate (Po) at a distance of between 0.5 cm and 5 cm above said open plate (Po), and the reduction factor of the porosity of each additional friction element (Pad) being between 0.6 and 0.9 relative to the porosity of an open plate (Po).
    [3]
    3. liquid-liquid extraction column according to claim 1 or 2, wherein the additional friction elements (Pad) have their orifices offset from those of the open plate (Po) to which it is attached, so as not to be in the same vertical axis.
    [4]
    4. liquid-liquid extraction column according to claim 1 or 2, wherein the weirs (D) of each weir tray (p1-p8) have a passage section of between 6% and 20% of the free section of column (1).
    [5]
    5. liquid-liquid extraction column according to claim 1 or 2, wherein the number of perforated trays spillways (p1-p8) is between 4 and 25, and preferably between 6 and 20.
    [6]
    6. Use of the liquid-liquid extraction column according to one of claims 1 to 5, for the extraction of sulfur compounds from a hydrocarbon phase with an aqueous sodium hydroxide solution representing from 10% to 20% by weight, the hydrocarbon phase being the dispersed phase.
    [7]
    7. Use of the extraction column according to one of claims 1 to 5, for a solute exchange between a heavy phase and a light phase in the case where the difference in density between the heavy phase and the light phase is greater than 300 kg / m3, and the density of the light phase is less than 750 kg / m3.
    类似技术:
    公开号 | 公开日 | 专利标题
    Li1971|Separation of hydrocarbons by liquid membrane permeation
    EP2349522B1|2015-02-25|Method for treating sea water with a view to producing injection water for undersea petroleum drilling, and corresponding equipment
    CA1325181C|1993-12-14|Nonmiscible liquids separator
    EP2773450B1|2015-07-29|Distributor plate for a gas/liquid mixture equipped with distributor elements largely insensitive to the lack of horizontality
    JP2019505378A|2019-02-28|Compact underwater dewatering
    US8425777B2|2013-04-23|Method of separating a mixture, and a plant for separating a mixture comprising water, oil and gas
    US20100326922A1|2010-12-30|Oil water separation apparatus
    JP2000061205A|2000-02-29|Liquid separation method and device therefor
    KR101781016B1|2017-09-25|Separation method for immiscible fluids
    CA2915280A1|2016-06-17|Compact distribution plate for gas/liquid contact columns at sea
    CH707291B1|2017-06-30|Liquid-liquid extraction column using trays equipped with a pressure drop generator element.
    EP3368173B1|2020-03-25|Column for heat and/or mass exchange between two fluids comprising a collection tray and fluid separation means
    EP1682257A1|2006-07-26|Method of mixing and distributing a liquid phase and a gaseous phase
    US6436290B1|2002-08-20|Method and apparatus for separating mixtures of organic and aqueous liquid phases
    CN108472557B|2021-05-07|Electrostatic technology system and method for dewatering crude oil in crude oil storage tanks of a floating production storage and offloading facility
    OA16784A|2016-01-04|Liquid extraction column using trays fitted with a pressure drop generator element.
    CA1135634A|1982-11-16|Apparatus for separating emulsions throughcoalescence
    CN108463277B|2021-11-30|Crude oil storage tank with electrostatic internals for dewatering crude oil in a processing train of a floating production storage and offloading facility
    US6824750B2|2004-11-30|Vertical extending liquid/liquid contacting column
    CH707268B1|2017-10-13|Liquid-liquid extraction column comprising two different types of trays.
    EP0768106B1|2004-01-21|Process for fractionating a fluid containing separable multi-components, e.g. a natural gas
    CN204745744U|2015-11-11|Liquid -liquid separation coalescer
    EP0252785A1|1988-01-13|Mixer-settler contact apparatus with a submerged gutter
    OA16783A|2016-01-04|Liquid extraction column comprising two types of distinct plates.
    WO2019120937A1|2019-06-27|Distributor tray with compartments and gas risers of the same shape for an offshore gas/liquid contact column
    同族专利:
    公开号 | 公开日
    KR102191956B1|2020-12-16|
    FR2998191A1|2014-05-23|
    US20140138285A1|2014-05-22|
    KR20140064670A|2014-05-28|
    FR2998191B1|2015-10-16|
    CH707291A2|2014-05-30|
    US10233397B2|2019-03-19|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2794711A|1955-11-17|1957-06-04|Exxon Research Engineering Co|Liquid-liquid countercurrent contacting device|
    US2872295A|1956-03-12|1959-02-03|Universal Oil Prod Co|Liquid-fluid contactor|
    US2895809A|1956-03-12|1959-07-21|Universal Oil Prod Co|Liquid-fluid contactor|
    US3354080A|1965-02-04|1967-11-21|Du Pont|Process for the removal of mercaptans from hydrocarbons|
    US4039389A|1975-11-03|1977-08-02|Uop Inc.|Liquid-liquid extraction apparatus|
    GB0910707D0|2009-06-19|2009-08-05|Weyland As|Method|
    US20120043259A1|2010-08-18|2012-02-23|Uop Llc|Extraction of Mercaptans in the Absence of Oxidation Catalyst|
    US9328294B2|2012-09-04|2016-05-03|Uop Llc|Process and apparatus for extracting sulfur compounds in a hydrocarbon stream|CN105753275B|2016-02-26|2018-12-11|山东科技大学|Oily sludge cleans harmless processing system|
    法律状态:
    2018-02-28| PCAR| Change of the address of the representative|Free format text: NEW ADDRESS: AVENUE DES MORGINES 12, 1213 PETIT-LANCY (CH) |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1203121A|FR2998191B1|2012-11-20|2012-11-20|LIQUID LIQUID EXTRACTION COLUMN USING TRAYS EQUIPPED WITH A LOAD LOSS GENERATING ELEMENT|
    [返回顶部]