WO2013081730A1 - Extraction par solvant - Google Patents

Extraction par solvant Download PDF

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Publication number
WO2013081730A1
WO2013081730A1 PCT/US2012/060330 US2012060330W WO2013081730A1 WO 2013081730 A1 WO2013081730 A1 WO 2013081730A1 US 2012060330 W US2012060330 W US 2012060330W WO 2013081730 A1 WO2013081730 A1 WO 2013081730A1
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WO
WIPO (PCT)
Prior art keywords
section
solvent
plural
feed
aromatic hydrocarbons
Prior art date
Application number
PCT/US2012/060330
Other languages
English (en)
Inventor
Arnold H. CHOI
John J. MONSON
Novica Rados
Original Assignee
Exxonmobil Chemical Patents Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Exxonmobil Chemical Patents Inc. filed Critical Exxonmobil Chemical Patents Inc.
Publication of WO2013081730A1 publication Critical patent/WO2013081730A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0426—Counter-current multistage extraction towers in a vertical or sloping position
    • B01D11/043—Counter-current multistage extraction towers in a vertical or sloping position with stationary contacting elements, sieve plates or loose contacting elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0488—Flow sheets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/30—Controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G75/00—Inhibiting corrosion or fouling in apparatus for treatment or conversion of hydrocarbon oils, in general
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1096—Aromatics or polyaromatics
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C10G2300/203—Naphthenic acids, TAN

Definitions

  • the present invention relates to hydrocarbon separation, and more particularly to liquid-liquid solvent extraction and a system adapted for the practice thereof.
  • Aromatic hydrocarbons such as benzene, toluene and xylenes (collectively, "BTX"), serve as important building blocks for a variety of plastics, foams and fibers. Often these compounds are produced via catalytic reformation of naphtha through steam cracking of naphtha or gas oils, or other methods where substantial amounts of non-aromatic compounds are present. When simple distillation or fractionation is not a cost effective or practical method for separation, liquid-liquid extraction techniques are used.
  • Such extraction techniques separate a desired substance selectively from a mixture or remove unwanted impurities from solution, and, in the present context of aromatic hydrocarbon separation from non-aromatic hydrocarbons, typically use a solvent which exhibits a higher affinity for the aromatic compounds than the non-aromatic compounds, thereby selectively extracting the aromatic compounds from the mixture of aromatics and non-aromatics.
  • the aromatic species of interest can then be isolated from the solvent by distillation, adsorptive separation techniques, crystallization techniques, and the like.
  • SulfolaneTM process developed by UOP, which is discussed in numerous patents and other literature too numerous to cite.
  • the process uses tetrahydrothiophene- 1,1 -dioxide (or sulfolane) as a solvent and water as a co-solvent.
  • Typical responses to correcting the decrease in capacity of the extractor include one or more of moving the recycle location, adding more stages of sieved trays, reducing operating rates, or cleaning and/or replacing the sieve tray decks.
  • Numerous other solutions have been disclosed, such as in U.S. Patent No. 7,288, 184, and U.S. Patent Application Publication No. 2010-0096321.
  • modifying the extractor tower internals significantly improves the separation of aromatic hydrocarbons from non-aromatic hydrocarbons, including liquid-liquid extraction processes and extractive distillation processes, can result, in embodiments, in at least an order of magnitude improvement in reliability (e.g., day-to-day ease of operation) and integrity (e.g., quicker response to unit upset) of the solvent systems and processes for the separation of aromatic hydrocarbons and non-aromatic hydrocarbons.
  • the invention concerns the control of solvent systems in processes and apparatus for the separation of aromatic hydrocarbons from non-aromatic hydrocarbons in liquid-liquid extraction, extractive distillation, and the combination thereof.
  • the invention concerns control of the build up of naphthenic impurities in the recycle of the solvent system and phase disengaging.
  • alteration of the tray and sieve arrangement improves one or more of phase separation, settling performance, and energy utilization in the liquid-liquid extractor unit.
  • layers of mono-filament, dual media crinkled wire mesh screen (DM-CWMS) and gratings are used to improve settling performance in the bottom section of the liquid-liquid extractor to minimize feed entrainment.
  • Figure 1 depicts a schematic view of an illustrative system for separating a hydrocarbon, according to one or more embodiments described.
  • Figures 2A, 2B, and 2C show details of gratings used in embodiments of the extractor unit of a process and apparatus according to the present invention.
  • Figures 3A, 3B, and 3C show details of the arrangement of demister pads in embodiments of the extractor unit according to the present invention.
  • Figure 4 illustrates details of a part of the extractor unit tower in embodiments of the present invention.
  • the invention concerns improvements in a process for liquid extraction which, in embodiments, improves the long term reliability of solvent systems, particularly in liquid- liquid extraction techniques for the separation of aromatic hydrocarbons from non-aromatic hydrocarbons.
  • the present inventors have noted that when processing feeds such as steam- cracked naphtha (SCN) and Reformate the recycle loop in a liquid-liquid extraction system can build up with naphthenic molecules, resulting in decreased capacity for extraction and higher than normal energy utilization.
  • One solution to minimize the recycle build up is to redesign the system so that the recycle piping is routed directly to the feed pipe or higher in the tower instead of the bottom of the extractor. This allows the naphthenic molecules to leave via the raffinate instead of the bottoms of the extractor.
  • Demister pads are per se known in the art and serve the function, at least in part, of a mist eliminator and/or to remove droplets from vapor. It has been surprisingly discovered that the layers of CWMS can be designed and spaced in such a manner as to prevent excessive change in pressure (dP) and/or mixing even in the case when they are plugged with foulant.
  • dP change in pressure
  • CWMS pads are advantageously positioned on gratings in the midsection of the extractor tower.
  • the grating material may cover the entire cross sectional area of the vessel.
  • the size of the grating is designed such that radial flow is minimized and axial flow maximized. This reduces unnecessary mixing in the extractor resulting in less feed entrainment.
  • sieve tray hole diameter for a few trays near (just above and/or below) the feed point, can be increased to minimize pluggage of sieve holes.
  • the sieve hole diameters get larger as they approach the feed line entry point.
  • the present invention is applicable to processes in which mixtures of aromatic and aliphatic (including cycloaliphatic) hydrocarbons are separated by extraction of the aromatic hydrocarbons and stripping the aromatic hydrocarbons from the extracting solvent. It is particularly applicable to the UOP SulfolaneTM process, which is a liquid-liquid extraction process to recover high-purity aromatics from hydrocarbon mixtures, such as reformate, pygas, or coke-oven light oil, and is discussed in patents and other literature too numerous to recite.
  • the extracting solvent is any liquid that preferentially extracts aromatic hydrocarbons over aliphatic hydrocarbons.
  • the boiling point of the extraction solvent should be higher than the boiling point of the aromatic hydrocarbons being extracted (i.e., it should have a boiling point of at least 100°C, and preferably between about 200°C and about 300°C) so that it is not evaporated during stripping.
  • the preferred extracting solvent is sulfolane, available as Sulfolane W® from Chevron Phillips Chemical Company, The Woodlands, TX, USA.
  • the solvent is selected from glycols, such as di-, tri-, and tetraethylene glycol, and nitrogen-containing species such as N-methyl pyrrolidine. Mixtures of such solvents can be used.
  • Figure 1 depicts a schematic view of an illustrative system 400 for separating a hydrocarbon mixture, according to one or more embodiments described.
  • the system 400 can further include one or more extractive distillation units (or strippers) 410, water strippers 420, water wash columns 430, and recovery columns 440.
  • the system 400 can further include one or more heat exchangers (three are shown 445, 450, 455), one or more steam generators 460, and one or more water/hydrocarbon separators (two are shown 465, 470).
  • a multicomponent hydrocarbon feed via line 145 (entering the extractor 100 at one or more locations) and a circulating solvent via line 150 can be contacted or otherwise mixed with one another.
  • this feed 145 is advantageously placed approximately at or above the bottom- most gratings 110 and at or below the trays.
  • the trays are not shown in Figure 1 for convenience of view; in that regard see Figure 4, where feed point 117 is approximately at or below the bottom of trays in section 118.
  • the feed entering the extraction unit and the circulating solvent have certain values with respect to TAN, free molecular oxygen, and chloride content.
  • the solvent extracts or otherwise separates at least a portion of the aromatic hydrocarbons from the multi-component hydrocarbon introduced via line 145 to provide a solvent enriched in aromatic hydrocarbons ("rich solvent”) via line 155 and a raffinate having a reduced content of aromatic hydrocarbons via line 160.
  • the solvent can include any suitable material suitable for separating aromatic compounds from non-aromatic compounds.
  • Illustrative solvents can include, but are not limited to tetraethylene glycol, triethylene glycol, diethylene glycol, ethylene glycol, methoxy triglycol ether, diglycolamine, dipropylene glycol, N-formyl morpholine, N-methyl pyrrolidone, 2,3, 4,5-tetrahydrothiophene- 1, 1 -dioxide ("sulfolane”), 3-methylsulfolane and dimethyl sulfoxide, tetramethylene sulfone, alone and/or in admixtures with water, and/or in combination with each other and/or water.
  • the solvent can have a pH ranging from a low of about 5, about 5.5, or about 6 to a high of about 8, about 8.5, or about 9.
  • the pH of the solvent in line 150 can range from about 5 to about 9, or about 5.5 to about 8, or about 6 to about 7.
  • the solvent is further distinguished from the aromatic and non-aromatic compounds by the characteristic that the aromatic compounds may be separated from the solvent by, for instance, steam stripping.
  • the hydrocarbon feed via line 145 is a mixture of aromatics and non-aromatics.
  • aromatics can include one or more C6-C9 aromatic hydrocarbons, including benzene, toluene, and/or xylene.
  • the hydrocarbon feed can be or include a product stream from catalytically reformed naphthas in which a C9 cut or extract of the reformate is enriched in C9 alkylbenzenes.
  • a typical composition of such C9 cut can contain about 2.5% mol C 8 , 87.5% mol C9 and 10% mol C 10 aromatics.
  • the hydrocarbon feed can be or include C6-C 9 aromatic hydrocarbons derived from gasoline producing processes such as the conversion of methanol to gasoline, as described in U.S. Patent Nos. 3,931,349, 3,969,426, 3,899,544, 3,894, 104, 3,904,916 and 3,894,102, and/or the conversion of synthesis gas to gasoline as described in U.S. Patent Nos. 4,096, 163, 4,279,830, 4,304,871 and 3,254,023.
  • the hydrocarbon feed can be or include C6-C 9 mixed aromatic hydrocarbons such as those derived from petroleum refinery sources, pyrolysis of coal to produce coke, tar sands, etc.
  • the hydrocarbon feed can be or include an alkylaromatic stream from a trans alky lation, isomerization, and/or disproportionation operation.
  • the volumetric solvent to hydrocarbon feed (S:H) ratio can range from about 1 : 1 , to about 5 : 1 , or from about 1 : 1 to about 3 : 1 , or from about 1 : 1 to about 2: 1. In at least one specific embodiment, the S:H ratio can be about 1.5: 1.
  • the solvent in line 150 can be introduced to the extractor 100 at a temperature ranging from a low of about 40°C, about 50°C, or about 60°C to a high of about 80°C, about 95°C, or about 100°C.
  • the temperature of the solvent in line 150 can range from about 60°C to about 85°C.
  • the extractor 100 can be operated at a pressure ranging from a low of about 225 kPa-g, about 250 kPa-g, or about 275 kPa-g to a high of about 400 kPa-g, about 450 kPa-g, or about 500 kPa-g.
  • the extractor 100 can be operated at a temperature ranging from about 40°C, about 50°C, or about 60°C to a high of about 70°C, about 85°C, or about 100°C.
  • the extractor 100 is operated at a temperate of from about 50°C to about 70°C.
  • the rich solvent in line 155 can have a hydrocarbon concentration ranging from a low of about 10% wt, about 15% wt, or about 20% wt to a high of about 30% wt, about 35% wt, or about 49% wt, with the balance being the solvent.
  • the aromatics in the rich solvent in line 155 can be about 50% wt, about 60% wt, about 70% wt, about 80% wt, or about 90% wt, with the balance being non-aromatic hydrocarbons.
  • the solvent concentration in the rich solvent in line 155 can range from a low of about 51% wt, about 65% wt, or about 70% wt to a high of about 80% wt, about 85% wt, or about 90% wt.
  • the rich solvent via line 155 can be introduced to the heat exchanger 445 to transfer heat from the lean solvent introduced via line 462 to provide a heated rich solvent via line 447 and a cooled lean solvent via line 150.
  • the heated rich solvent via line 447 can be introduced to the stripper 410 to provide a less-aromatic rich hydrocarbon via line 412 and a solvent further enriched in aromatic hydrocarbons via line 414.
  • the raffinate in line 160 can have a non-aromatic hydrocarbon concentration ranging from a low of about 80% wt, about 85% wt, or about 90% wt to a high of about 95% wt, about 97% wt, about 98% wt, or more.
  • the raffinate in line 160 can have an aromatic hydrocarbon concentration ranging from a low of about 0.5% wt, about 1% wt, or about 3% wt to a high of about 5% wt, about 10% wt, or about 20% wt.
  • the raffinate in line 160 can have a solvent concentration ranging from a low of about 0.1% wt, about 0.25% wt, or about 0.5% wt to a high of about 0.75% wt, about 1% wt, or about 2% wt.
  • the raffinate in line 160 can be introduced to the raffinate wash column 430 to provide a raffinate product lean in solvent (sulfolane) via line 432 and a recovered water/solvent stream via line 434.
  • the raffinate wash column 430 can separate at least a portion of the solvent in the raffinate to provide a raffinate product via line 432 containing less solvent than the raffinate in line 160.
  • the recovered water/solvent in line 434 can contain aromatics/non-aromatics separated in/entrained from the raffinate wash column 430 from the raffinate introduced via line 160.
  • the recovered water/solvent in line 434 can be introduced to the water stripper 420 to provide a water-lean, hydrocarbon-rich stream via line 422.
  • the non-aromatic rich raffinate via line 432 can be further processed or sent to storage.
  • the water-lean, hydrocarbon-rich stream in line 422 can be introduced to the water/hydrocarbon separator 470 to provide a recycle hydrocarbon via line 472 and a recovered water stream via line 474.
  • the recycle hydrocarbons via line 472 can be introduced to the first section 120, and/or the second section 130, and/or the third section 140 of the extractor 100 for additional processing.
  • the recycle hydrocarbon via line 472 can be mixed with the feed line 145.
  • the bottoms from the stripper 410 is contacted with steam to recover the aromatics.
  • the aromatic compounds are removed from the top of the recovery column 440 and the bottom stream (lean solvent) 462 is recycled back to the extractor 100, although a portion maybe sent to solvent regenerator 442.
  • 443 is a mixture of solvent and water (as a liquid or vapor) and is the "regenerated solvent”.
  • the bottoms collects heavy acid salts and other solids and is purged periodically.
  • the overhead from the recovery column 440 is introduced to the water/hydrocarbon separator 465 to separate the water via line 467 from the product aromatics via line 466. At least a portion of the recovered aromatics can be recycled to the recovery column 440 as reflux and all or a remaining portion of the product is recovered through conduit 550.
  • the recovered water is sent to the water wash column 430.
  • the extractor 100 length to diameter (L/D) ratio can be selected by one of ordinary skill in the art in possession of the present disclosure. For clarity and ease of description, the extractor 100 will further be described with reference to a vertical, cylindrical vessel having an L/D ratio of greater than 1.
  • FIG. 1 Three sections or volumes within extractor 100 are depicted in Figure 1, namely a first section ("aromatics recovery section") 120, which generally comprises trays (not shown for convenience of view in Figure 1 but illustrated partially in Figure 2, discussed below), a second section (“feed section”) 130, and a third section (“aromatics purity section”) 140, each section in fluid communication with one another.
  • a first section (“aromatics recovery section") 120, which generally comprises trays (not shown for convenience of view in Figure 1 but illustrated partially in Figure 2, discussed below)
  • feed section feed section
  • aromatics purity section each section in fluid communication with one another.
  • the first section 120 is disposed above the second section 130, and includes one or more trays disposed therein, which are not shown in Figure 1 for convenience of view.
  • plural trays 1 18 in section 120 can include, but are not limited to sieve trays, rotating discs, perforated trays, bubble cap trays, floating valve trays, fixed valve trays, tunnel trays, cartridge trays, dual flow trays, baffle trays, shower deck trays, disc and donut trays, orbit trays, horse shoe trays, cartridge trays, snap-in valve trays, chimney trays, slit trays, shed trays, or any combination thereof.
  • the plural trays 1 18 are sieve trays containing a plurality of circular openings.
  • Each opening can have a diameter ranging from a low of about 3 mm, about 4 mm, about 5 mm, about 6 mm, about 7 mm, or about 8 mm to a high of about 9 mm, about 10 mm, about 1 1, about 12, about 13, about 14, about 15, about 16, about 17, about 18, about 19, about 20, about 21, about 22, about 23, about 24, or about 25 mm.
  • the various inlets and outlets in Figure 4 are not shown for convenience of view but one of ordinary skill in the art in possession of this disclosure would be able to arrange these appropriately.
  • the second section 130 is located between the first and third sections 120, 140, and is in fluid communication with one or more hydrocarbon feed inlets 145.
  • the second section 130 comprises plural gratings 110, described in more details herein, such as with reference to Figures 2A, 2B, and 2C, but is otherwise preferably devoid of any sieve trays such as in section 120 or packing material.
  • the plural gratings 110 provide a better coalescing surface area for separation and additional open area to mitigate fouling.
  • the second section 130 can include a single grate, in preferred embodiments there are plural gratings, such as the three shown in Figure 1, or there can be two or four or more gratings 1 10, depending on design criteria, feed specifications, and product specifications.
  • the vertical spacing between the gratings 110 can also vary, depending on design criteria, feed specifications, and product specifications.
  • the vertical spacing (“n" in Figure 3A) can vary anywhere from about 0.25 m to about 10 m; preferably 0.25 m to 5 m; and more preferably, 0.25 m to 0.5 m.
  • the third section 140 is disposed below the second section 130.
  • the third section 140 is in fluid communication with one or more rich solvent outlets 155.
  • the third section 140 can include one or more vortex breakers (not shown) and/or packing materials (not shown), and also optionally trays and/or grids (also not shown), and in preferred embodiments section 140 comprises plural demister pads 115 disposed therein on conventional supports, such as "T" beams, per se known in the art.
  • the arrangement of the demister pads 1 15 is better illustrated with respect to Figures 2A, 2B, and 2C, described further below.
  • packing material can be in one or more of the first section 120, second section 130, and third section 140.
  • packing material can include, but is not limited to one or more types of structured and/or random shaped materials.
  • the packing material can increase the effective surface area within the extractor 100, increasing the mass transfer between liquid and gas phases.
  • Suitable packing materials can include one or more metals, metal alloys, ceramics, composites or other non-metals, polymers, glass, or any combination thereof.
  • suitable packing materials can be or include one or more Raschig rings, Lessing rings, I-rings, saddle rings, Intalox saddles, Tellerettes, Pall rings, U-rings, or any combination thereof.
  • Illustrative examples of commercially available structured packing includes, but are not limited to, Flexipac and Gempak structured packings as manufactured by the Koch-Glitsch Corporation, corrugated sheets, crimped sheets, gauzes, grids, wire mesh, monolith honeycomb structures, or any combination thereof.
  • the demister pads 115 can be or include a mesh screen, preferably one or more crinkled wire mesh screens ("CWMS"). Suitable CWMS can be made from interwoven or inter-twined strips of wire or multiple types of wire.
  • the wire mesh can be made from steel, stainless steels, TeflonTM, or other similar materials.
  • the wire may be coated with a non-polar material such as TeflonTM.
  • the demister pads comprises a monofilament of TeflonTM and a monofilament of stainless steel woven into a mesh.
  • Each pad 115 can have the same dimensions or the dimensions of each pad 1 15 can be different and independent of one another.
  • each pad 1 15 can range in length from about 0.5 m, 1.0 m, or 3 m to about 5 m, 10 m, or 15 m.
  • Each pad 115 can range in width from about 0.1 m, 0.5m, or 1 m to about 1.5 m, 2 m, or 5 m.
  • Each pad 115 can range in height from about 0.1 m, 0.5 m, or 1 m to about 1.5 m, 2 m, or 5 m.
  • the present inventors have discovered an improved array of the demister pads as compared with that in the prior art, in that, as shown in Figures 1, 3, and 4, the array of demister pads is staggered from layer to layer.
  • the present inventors have surprisingly found that the staggered pattern allows for liquid flow even in the event the CWMS/demister material plugs with solids and also promotes axial flow versus mixing.
  • staggered is meant that the array of demister pads for each succeeding layer of pads, whether disposed on gratings as in the middle section or in the bottom section, supported by conventional supports such as "T" beams, is such that a demister pad on one level is disposed substantially over an opening in the next layer, and so on. This is shown, for instance, in Figure 3A.
  • FIG. 2A depicts a plan or horizontal view from the top of an illustrative feed grating or grating 110, according to one or more embodiments.
  • Figures 2B and 2C depicts two embodiments of a side or cross-sectional view of the same, showing grid sections 113a and 113b, respectively, and openings 110a and 110b, respectively.
  • the feed grating 1 10 can be a monolithic structure containing a plurality of openings or passageways (1 10a or 1 10b) formed therethrough.
  • each grating 1 10 has at least 50 % open area.
  • each grating 110 has at least 75 % open area.
  • each grating 1 10 has at least 90 % open area.
  • the dimensions of x, y, z and angle m can be determined by one of ordinary skill in the art in possession of the present disclosure, however, assuming, in a preferred embodiment, that the diameter of the grating 110 is approximately 450 to 500 cm and is approximately the same diameter of the tower (thus extended over the entire cross-sectional area of the tower), x will range from about .1 to .4 cm, y will range from about 1 to 3 cm, z will range from about 2 to 5 cm, and m will range from about 30 to about 60° measured from the base, i.e., along the diameter.
  • Each opening 110a or 110b can be triangular, square, rectangular, elliptical, circular, oval, or any other shape.
  • each opening 113a or 113b in Figures 2B and 2C, respectively has, in embodiments, a polygonal cross-section having at least three sides.
  • each opening is rectangular, as depicted in Figure 2A, to provide a grid pattern resembling that of pedestrian grating or subway grating.
  • each opening 1 13a or 113b in Figures 2B and 2C, respectively can range from a low of about 0.5 cm, about 1 cm, about 1.5 cm, or about 2 cm to a high of about 3 cm, about 5 cm, about 7 cm, or about 10 cm.
  • the height of each opening 215 can range from a low of about 0.5 cm, about 1.0 cm, or about 1.5 cm, to a high of about 2 cm, about 3 cm, about 5 cm, or about 10 cm.
  • the cross-section area of each opening can be the same or different.
  • the openings 1 13a in Figure 2B disposed about the periphery of the feed grating can be smaller or larger than the openings of the grating disposed about a central portion of the feed grating.
  • different sized openings can be randomly distributed or arranged in a certain pattern, such as a circular, spiral, or square shaped pattern, across the grating. As previously mentioned, it is advantageous from the standpoint of avoiding fouling that the opening in gratings near the feed entry point are larger when compared with the openings in gratings further away from said feed entry point.
  • Figure 4 depicts a cross sectional view of the extractor tower showing the first section 1 18 comprised of plural trays, middle section 1 16 comprised of gratings having demister pads thereon, and bottom section 115 comprised of demister pads.
  • Feed point 117 is preferably positioned near, at, or below the last tray in section 118.
  • each feed grating 1 10 can be at least partially coated, in addition to having demister pads disposed thereon.
  • the one or more feed gratings 110 can be at least partially coated with one or more non-polar materials to provide additional coalescing contact area.
  • the non-polar coating can attract or otherwise have an affinity for the non-aromatic hydrocarbons, also non-polar, which can further promote the separation of the aromatic hydrocarbons from the non-aromatic hydrocarbons.
  • the one or more non-polar coatings should also be compatible with aromatic hydrocarbons.
  • Suitable coating materials can include, for example, fluoropolymers, such as TeflonTM, and epoxy-containing polymers.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne une séparation d'hydrocarbures, et plus particulièrement, une extraction par solvant liquide-liquide et un système apte à la mise en œuvre de celle-ci, ce par quoi l'un des résultats suivants est obtenu : la performance de sédimentation est améliorée, l'encrassement interne d'une tour est diminué, l'écoulement radial est diminué, et l'écoulement axial est augmenté.
PCT/US2012/060330 2011-12-02 2012-10-16 Extraction par solvant WO2013081730A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201161566116P 2011-12-02 2011-12-02
US61/566,116 2011-12-02

Publications (1)

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WO2013081730A1 true WO2013081730A1 (fr) 2013-06-06

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108697947A (zh) * 2015-12-25 2018-10-23 可口可乐公司 提取物生产系统及用于生产提取物的方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4325888A (en) * 1978-01-13 1982-04-20 Propylox Preparation of peracid by liquid-liquid extraction
US4336106A (en) * 1980-10-17 1982-06-22 Uop Inc. Apparatus for the solvent extraction of aromatic hydrocarbons from a hydrocarbon mixture
US4686089A (en) * 1985-02-26 1987-08-11 Wiederaufarbeitungsanlage Karlsruhe Betriebsgesellschaft Mbh Sieve-plate column for counterflow extraction
US20060124509A1 (en) * 2004-12-10 2006-06-15 Van Nuland Marcus Lambertus H Process for mitigating acids in a system for separating aromatic hydrocarbons from a hydrocarbon feedstream
US20100096321A1 (en) * 2008-10-20 2010-04-22 Monson John J Apparatus and Methods for Separating a Hydrocarbon

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4325888A (en) * 1978-01-13 1982-04-20 Propylox Preparation of peracid by liquid-liquid extraction
US4336106A (en) * 1980-10-17 1982-06-22 Uop Inc. Apparatus for the solvent extraction of aromatic hydrocarbons from a hydrocarbon mixture
US4686089A (en) * 1985-02-26 1987-08-11 Wiederaufarbeitungsanlage Karlsruhe Betriebsgesellschaft Mbh Sieve-plate column for counterflow extraction
US20060124509A1 (en) * 2004-12-10 2006-06-15 Van Nuland Marcus Lambertus H Process for mitigating acids in a system for separating aromatic hydrocarbons from a hydrocarbon feedstream
US20100096321A1 (en) * 2008-10-20 2010-04-22 Monson John J Apparatus and Methods for Separating a Hydrocarbon

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108697947A (zh) * 2015-12-25 2018-10-23 可口可乐公司 提取物生产系统及用于生产提取物的方法

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