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US3167501A - Process for solvent refining hydrocarbon oils - Google Patents

Process for solvent refining hydrocarbon oils Download PDF

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US3167501A
US3167501A US124839A US12483961A US3167501A US 3167501 A US3167501 A US 3167501A US 124839 A US124839 A US 124839A US 12483961 A US12483961 A US 12483961A US 3167501 A US3167501 A US 3167501A
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solvent
oil
boiling
line
water
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US124839A
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Robert A Woodle
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Texaco Inc
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Texaco Inc
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • 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

Definitions

  • This invention is directed to a hydrocarbon treatment process employing liquid-liquid solvent extraction. More particularly, it relates to a method of solvent refining hydrocarbons containing a small portion of constituents co-boiling with the solvent.
  • hydrocarbon oils containing constituents co-boiling with the solvent are contacted with a solvent forming separate extract and ratlinate phases.
  • the extract phase or a portion thereof is distilled in the presence of a relatively high boiling hydrocarbon oil under extractive distillation conditions effecting separation of solvent free of co-boiling hydrocarbons from bottoms comprising extracted oil in adrnixture with said relatively high boiling hydrocarbon oil.
  • lailnate is disstilled in the presence of steam under azeotropic distillation conditions to elfect separation of solvent from refined oil. Extractive distillation bottoms are distilled in the presence ofsteam under azeotropic distillation conditions to effect separation of remaining solvent from the hydrocarbons or extracted hydrocarbons and remaining solvent from the relatively high boiling hydrocarbons.
  • extractive distillation is combined with azeotropic distillation to eliect a high degree of separation of co-boiling oils from solvent in a solvent extraction process.
  • the treating process of this invention is applicable to a Wide range of hydrocarbon oils, for example, it may be applied to the manufacture of lrerosenes, diesel fuels, gasoil cracking stocks, light lubricating oil stocks, hydraulic oils, oils suited for the preparation of specialty products, and oils suited for chemical manufacture.
  • furfural is a preferred solvent useful in the process of this invention, other solvents may be employed which are partially miscible with water at about 100 F. and
  • solvents include for example, other furans, nitrobenzene, amines for example, aniline, ketones, for example 3-pentanone and mcsityl oxide, hydroxy compounds, for example phenol and n-amyl alcohol, aldehydes, for example, benzaldehyde, nitriles, for example, propionitrile and butyronitrile, and esters, for example n-butyl acetate and n-amyl acetate.
  • the solvent used may comprise a mixture of several individual solvents and the solvent may be modir'ied by the inclusion of antisolvents, for example water.
  • distillative separation of solvent from dissolved hydrocarbons is effected in the presence of a relatively high boiling hydrocarbon oil.
  • the presence of the high boiling oil reduces the relative volatility of the co-boiling components of the dissolved oil so that solvent free of coboiling hydrocarbons may be removed as distillate and all of the oil initially dissolved in the solvent is removed as bottoms with the relatively high boiling oil.
  • the extractive distillation is effected at a pressure selected to augment the effect of the high boiling oil on the relative volatility of the co-boiling hydrocarbon and to achieve optimum and most economical equipment design and operation. Preferred pressures in the extractive distillation step, depending upon the hydrocarbon oil feed,
  • the relatively high boiling oil itself should be free of components boiling in the region of the solvent and preferably should consist of components having true boiling points at least F. above the boiling range of the solvent. In some cases, the relatively high boiling oil may be used on a once through basis and 'discharged with the dissolved oil in which case the boiling ranges of the two oils may overlap. Generally, however, it is desirable to separate the dissolved oil as a separate product by distillation, in which case, the relatively high boiling il should consist of components boiling wholly above the treated oil. Suitable high boiling oils include both distillates and residua. A paraflinic residium boiling wholly above 760 F. at atmospheric pressure is preferred for use as a relatively high boiling oil when treating oils boiling within the range of about 350 to 700 F. by ASTM distillation.
  • FGURE l is a flow diagram of one form of the process of this invention adapted primarily to the refining of relatively low boiling oils.
  • FIGURE 2 is a liow diagram of an embodiment of this invention in an apparatus useful for the solvent treatment of both light and heavy hydrocarbonv oils.
  • a light lubricating oil stock is charged through line il to extraction tower 2.
  • extraction tower 2 the oil is countercurrently contacted with solvent introduced into the top of tower Z through line 3.
  • the solvent may suitably be wet furfural, that is, liquid furtural containing a small amount of dissolved water.
  • Raiinatemix comprising'retined light lubricating oil stock and a small amount of dissolved solvent is vwithdrawn through line 4 and passed to rafnate stripper 7.
  • the azeotropic mixture in line comprises vapors of solvent, water, and a small amount of hydrocarbon oil.
  • the vapor mixture is condensed in cooler 15 and therresulting condensate is passed through line 16 to separator 17.
  • Three liquid phases separate, that is an oil phase containing a small amount of dissolved solvent and water, a water phase containing a small amount of dissolved solvent and oil, and a solvent phase containing a small amount of water and oil.
  • Separator 17 is provided with internal batlles indicated by dotted lines 1S and 19 to permit separate withdrawal of the three phases.
  • Separated solvent phase is withdrawn through line 2@ and returned to extraction tower 2 through line 3.
  • arated water phase is withdrawn through line 21 for subsequent solvent recovery.
  • Separated oil phase is withdrawn through line 22, passed to washer 23 and countercurrently contacted with water therein introduced through line 24.
  • Oil free of solvent is withdrawn through line 25 and combined with the rened oil in line 11 to provide a solvent reiined light lubricating oil stock product of the process.
  • Water washings from washer 23 are withdrawn through line 26 and combined Sepwith the water phase in line 21 for subsequent solvent recovery.
  • Extract-mix comprising solvent and dissolved extracted oil is Withdrawn from the bottom of tower 2 through line 30. Extract-mix is cooled in cooler 31 land the cooled stream is passed through line 32 to settler 33. A secondary rarinate phase separates from the remaining extractmix in settler 33. This separated secondary ratinate contains a small amount of dissolved solvent and is withdrawn through line 36 and passed to wash tower 37 where it is countercurrently contacted with water intro- -duced through ⁇ line 33. Water washings are withdrawn through line 4t) for'subsequent solvent recovery. Washed secondary rainate is withdrawn through line 39 as a part ofV the extract product of the process discharged through line 41.
  • extractive distillation tower 59 the hydrocarbon and solvent Yvaporsvare distilled in contact with a relat'ively high". boiling hydrocarbon oil introduced into the top of tower through line 5S. By distilling the solvent a-nd extract vapors in Contact with the high boiling oil, the extract vapors are condensed in the high boiling oil and solvent free of oil is removed as distillate through line 56.
  • the extractive distillation tower bottoms, comprising the high boiling oil, extract oil, and a part of the solvent, are withdrawn through line 57 and passed to extract stripping tower 53.
  • VOil phase containing a small arount of dissolved water and solvent is withdrawn through line 72 and combined with the oil in line 36 for water washing and recovery.
  • Separated water phase is withdrawn through line 71, combined with water streams in lines 21 and Alti and passed to fractionator 75 for recovery of dissolved solvent.
  • Solvent phase is withdrawn through line ⁇ 76 and recycled with the extract-mix in line 32 through the settler, flash drum and extractive distillation circuit.
  • Solvent vapors substantially free of oil in line 56 are condensed in cooler 77 and passed through line. 7S to water-solvent separator 79. Water phase separating in separator 79 is withdrawn through line 30 and passed to fractionator 75 for recovery of dissolved solvent. leparated solvent phase is passed through line S5 to accumulator Se from which solvent is withdrawn .through line 3 for charge to extraction tower 2.
  • Fractionator 75 is employed to recover solvent dissolved in water from the water discharged from the systent
  • the azeotrope vapor stream is combined with the vapor stream in line 56 for condensation, separation or solvent phase, and return to the extraction system. Water free of solvent is Withdrawn through line 8S for discharge from the system.
  • FGURE 2 illustrates a method of integrating the process of this invention into a system useful in the solvent refining of a full range of hydrocarbon oils including both oils containing solvent co-boiling components and oils wholly boiling substantially above the boiling range of the solvent.
  • charge oil is introduced through line 101 into tower 102 and contacted countercurrently with solvent introduced through line 103.
  • Raf. inate-mix withdrawn through line 105 is passed to rened oil stripper 1% where the solvent is removed by stripping with steam introduced through line 1417.
  • Azeotropic mixture of steam and solvent is withdrawn through line 11@ for solvent recovery and reconcentration as will be described hereinafter.
  • Rened oil is Vwithdrawn through line 111.
  • Extract-mix is withdrawn through line and passed to solvent iiash tower 121.
  • the bulk of the solvent is removed as vapor free of oil through line 122 and passed to solvent drying tower 131 described hereinafter.
  • Flashed extract-mix containing a small amount of residual solvent is passed through line 123 to stripper 124 wherein it is contacted with steam introduced through line 127 to remove residual solvent.
  • An azeotropic mixture of solvent and water vapor is withdrawn through line for reconcentration and recovery. Extract free of solvent is withdrawn through line 126.
  • Solvent is recovered and concentrated in a distillation system comprising solvent recovery tower 130 and solvent solvent drying tower 131.
  • solvent drying tower 131 water is removedtrom the solvent by distilling all of the water overhead as the low boiling azeotrope which is discharged through line 31139 and combined with the azeotrope vapors in line 132 for condensation and phase separation. Solvent free of water is withdrawn from the bottom of tower 131 for recycle to extraction tower 102 through line .103.
  • both the raiiinate-mix in line 105 and the extract mix in line 120 may contain constituents co-boiling with the solvent.
  • Low boiling constituents in the raiiinate-mix appear in the distillate from refined oil stripper 106, along with the azeotropic mixture of steam and solvent.
  • This vapor mixture is withdrawn through line M and 11h11 to cooler 150.
  • Condensed distillate is passed through line il to separator l52 whe-rein oil, water and solvent phases are separated. Oil phase is withdrawn through line 153 and passed to washer 155 wherein it is countercurrently contacted with water introduced through line 154.
  • Light refined oil is discharged through line H6 and may be combined with the refined oil from line 111 as the reiined oil product of the process.
  • Water washings are withdrawn from the bottom of tower 155 through line 166, combined with water phase withdrawn from separator 152, and the mixture passed through line 161 to solvent recovery tower 130.
  • Extract-mix containing constituents co-boiling with the solvent is withdrawn from tower 102 through line 125B and passed through line 12W to extractive distillation tower lofi Relatively high boiling oil is introduced to the top of tower 165 through line 166.
  • Extract-mix is distilled in tower 16S under conditions effecting removal of the bulk of the solvent as an overhead distillate substantially free of hydrocarbon oil.
  • Solvent vapor is discharged through line 167 and combined with the stream passed through line 125 for solvent recovery and concentration. Extractive distillation tower bottoms comprising a relatively small amount of solvent, the extract oil, and the relatively high boiling oil are withdrawn through line 170 and passed to tower 124.
  • Extractive distillation tower bottoms are distilled in tower i224 with steam introduced through line 127 under conditions etiecting vaporization and distillation of remaining solvent and extract oil which are discharged through lines 25 and 12551 to condenser 171.
  • Condensed distillate is discharged through line 172 to separator 1173.
  • Oil, Water and solvent phases are separated in separator 173.
  • Oil phase is withdrawn through line 175 to washer 176 wherein it is countercurrently contacted with water introduced through line 177.
  • Extract product of the process is discharged through line 178.
  • Water washings are withdrawn from the bottom of washer 176 through line 179, combined with water phase withdrawn from separator 173 in line lh, and the mixture passed to solvent recovery tower 130.
  • Separated solvent phase is withdrawn from separator 173 through line 190 and returned to the feed to extractive distillation tower in adniixture with the extract-mix in line 120g.
  • Example K illustrates the application of the process of this invention to the reiining of a light lubricating oil stock useful in the manufacture of hydraulic oils.
  • ilow rates are expressed in terms of liquid barrels per hour regardless of whether the particular stream is in the liquid or vapor form.
  • a lubricating oil charge stock having an ASTM distillation initial boiling point of 440 F., a 50 percent point of 490 F., and an endpoint of 632 F. at a rate of 18.7 barrels per hour is countercurrently contacted with 49.4 barrels per hour of solvent having a composition of 90 percent furfural, 9 percent water and 1 percent oil. Extraction is eected with a top tower temperature of 17l F.
  • Raiiinate-rnix at a rate of 15.3 barrels per hour is steam stripped at a top tower temperature of 208 F. to produce 12.7 barrels per hour of oil bottoms free of solvent and an overhead azeotropic distillate.
  • the azeotropic distillate is condensed separating 1.7 barrels per hour of solvent phase comprising '86 percent furfural, 3 percent oil, and 1l percent water, 5.4 barrels of water phase comprising 92 percent water and 8 percent furfural and .4 barrel or" oil phase comprising percent oil, 18 percent furtural and 2 percent water.
  • the solvent phase is returned as part of the solvent passed to the extraction tower, the water phase is directed to the solvent recovery equipment, and the oil phase is water washed and combined with the raiinate stripper bottoms to produce 13.0 barrels per hour of reiined oil product.
  • Extract-mix at a rate of 52.8 barrels per hour comprising 80 percent furfural, l2 percent extract oil, and S percent' water together with 4.8 barrels of recovered solvent as hereinafter provided comprising 75 percent turtural, 15 percent oil, and 10 percent water are cooled to 105 F. effecting separation of .5 barrel per hour ot secondary ratlinate which is water washed to provide a part of the extract product of the process. Remaining extract-mix is heated to 325 F. and dashed from a residue of 0.8 barrel per hour of extract. Flashed vapors equivalent to 56.2 barrels per hour are passed to an extractive distillation tower operated at atmospheric pressure and a top tower temperature of 325 F.
  • a heavy paraliinic residual oil boiling wholly above 760 F. at atmospheric pressure is reiluxed to the top of the extractive distillation tower at a rate of 56.2 barrels per hour. Extractive distillation tower overhead at a rate of 46.2 barrels per hour comprising 89 percent furfural, 10 percent water and 1 percent oil is condensed and passed to a furfural-water settler.
  • Extract distillation tower bottoms at a rate ot 66.2 barreis per hour comprising 8 percent extract, 7 percent furtural kand percent heavy oil is passed to an extract stripper.
  • the extractive distillation tower bottoms are stripped with 12.7 barrels per hour or" steam at' a top tower temperature of 208 F. to separate 56.2 barrels per hour of heavy oil as bottoms for recycle to the extra/:tive distillation tower and 22.7 barrels per hour of distillate. Distillate is condensed to form oil-rich, water-rich and turfural-rich phases.
  • Furfural phase at a rate of 4.8 barrels per hour comprising 75 percent furfural, l5 percent oil and l0 percent water is withdrawn and adrnixed with the extract-mix passed to the extractive distillation tower.
  • Water at a rate of 13.2 barrels per hour containing 8 percent turfural is passed to a water from urfural fractionator for the recovery of furural.
  • Oil phase at a rate of 4.7 barrels per hour is withdrawn, water washed, and combined with the secondary raffinate and the extract-mix ashed residue to produce 5.8 barrels per hour of extract product.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Description

Jan. 26, 1965 R, A. wooDLE PROCESS FOR SOLVENT REFINING HYDROCARBON OILS Filed July 18, 1961 v 2 Sheets-Sheet 1 Jan. 26, 1965 R. A. wooDLE PROCESS FOR soLvENT REFINING HYDRocARsoN ons 2 Sheets-Sheet 2 Filed July 18, 1961 ein This invention is directed to a hydrocarbon treatment process employing liquid-liquid solvent extraction. More particularly, it relates to a method of solvent refining hydrocarbons containing a small portion of constituents co-boiling with the solvent. ln accordance with the process of this invention, hydrocarbon oils containing constituents co-boiling with the solvent are contacted with a solvent forming separate extract and ratlinate phases. The extract phase or a portion thereof is distilled in the presence of a relatively high boiling hydrocarbon oil under extractive distillation conditions effecting separation of solvent free of co-boiling hydrocarbons from bottoms comprising extracted oil in adrnixture with said relatively high boiling hydrocarbon oil. lailnate is disstilled in the presence of steam under azeotropic distillation conditions to elfect separation of solvent from refined oil. Extractive distillation bottoms are distilled in the presence ofsteam under azeotropic distillation conditions to effect separation of remaining solvent from the hydrocarbons or extracted hydrocarbons and remaining solvent from the relatively high boiling hydrocarbons.
In solvent refining processes wherein the solvent and material treated have substantially dierent boiling ranges, the solvent is readily separated from the extract and ramnate phases by simple distillation. However, separation by simple distillation is incomplete when the oil treated contains components having true boiling points in the region of the boiling point or boiling range of the solvent. For example, hydrocarbon oils having initial boiling points by ASTM distillation of less than about 625 F. may contain some components having true boiling points as low as about 325 F. Therefore, in treating hydrocarbon oils having initial boiling points by ASTM distillation less than about 625 F. with furfural as a solvent, oils co-boiling with the furfural tend to accumulate in the solvent thereby reducing its solvent power and its selectivity for extraction. Heretofore, it has been proposed that these co-boiling hydrocarbons be separated from solvents by azeotropic distillation wherein a low boiling azeotrope of solvent and water is distilled from the hydrocarbon. However, azeotropic distillation of the entire solvent stream circulated in the treating process requires an inordinately large amount of steam. Additionally, although azeotropic distillation is effected at a temperature substantially below the temperature of the boiling point of the pure solvent, substantial amounts of low boilingr hydrocarbons may be vaporized with the azeotrope particularly when treating relatively low boiling stocks such as kerosene, diesel fuel, and hydraulic oils.
ln `accordance with the process of this invention, extractive distillation is combined with azeotropic distillation to eliect a high degree of separation of co-boiling oils from solvent in a solvent extraction process. The treating process of this invention is applicable to a Wide range of hydrocarbon oils, for example, it may be applied to the manufacture of lrerosenes, diesel fuels, gasoil cracking stocks, light lubricating oil stocks, hydraulic oils, oils suited for the preparation of specialty products, and oils suited for chemical manufacture. Although furfural is a preferred solvent useful in the process of this invention, other solvents may be employed which are partially miscible with water at about 100 F. and
ldlm
liatenteel dan. 26, lg
which are capable of forming an azeotrope with water. Such solvents include for example, other furans, nitrobenzene, amines for example, aniline, ketones, for example 3-pentanone and mcsityl oxide, hydroxy compounds, for example phenol and n-amyl alcohol, aldehydes, for example, benzaldehyde, nitriles, for example, propionitrile and butyronitrile, and esters, for example n-butyl acetate and n-amyl acetate. As is well known in the art, the solvent used may comprise a mixture of several individual solvents and the solvent may be modir'ied by the inclusion of antisolvents, for example water.
in the extractive distillation step of this invention, distillative separation of solvent from dissolved hydrocarbons is effected in the presence of a relatively high boiling hydrocarbon oil. The presence of the high boiling oil reduces the relative volatility of the co-boiling components of the dissolved oil so that solvent free of coboiling hydrocarbons may be removed as distillate and all of the oil initially dissolved in the solvent is removed as bottoms with the relatively high boiling oil. The extractive distillation is effected at a pressure selected to augment the effect of the high boiling oil on the relative volatility of the co-boiling hydrocarbon and to achieve optimum and most economical equipment design and operation. Preferred pressures in the extractive distillation step, depending upon the hydrocarbon oil feed,
- the solvent, and the relatively high boiling oil employed,
may be within the range of less than atmospheric, that is, a vacuum, up to about live atmospheres or higher.
The relatively high boiling oil itself should be free of components boiling in the region of the solvent and preferably should consist of components having true boiling points at least F. above the boiling range of the solvent. In some cases, the relatively high boiling oil may be used on a once through basis and 'discharged with the dissolved oil in which case the boiling ranges of the two oils may overlap. Generally, however, it is desirable to separate the dissolved oil as a separate product by distillation, in which case, the relatively high boiling il should consist of components boiling wholly above the treated oil. Suitable high boiling oils include both distillates and residua. A paraflinic residium boiling wholly above 760 F. at atmospheric pressure is preferred for use as a relatively high boiling oil when treating oils boiling within the range of about 350 to 700 F. by ASTM distillation.
lt is an object of this invention to provide a means of treating hydrocarbon oils containing constituents coboiling with the solvent. Other objects Will be apparent from the following description and claims. An advantage of the process of this invention is that the oil content of the solvent stream is maintained at a desirably low level thereby maintaining high solvent efficiency. Another advantage of this invention is that the oil content of the circulating solvent is maintained at a low level without requiring extremely high steam consumption. Another advantage of this invention is that separation of oil is effected without chilling or dilution and with a minimum of reconcentration Kof the solvent.
FGURE l is a flow diagram of one form of the process of this invention adapted primarily to the refining of relatively low boiling oils.
FIGURE 2 is a liow diagram of an embodiment of this invention in an apparatus useful for the solvent treatment of both light and heavy hydrocarbonv oils. Although the drawings illustrate arrangements of apparatus in which the process of this invention may be practiced, it is not intended to limit the invention to the particular apparatus or materials described.
Referring Ito FlGURE l, a light lubricating oil stock is charged through line il to extraction tower 2. ln extraction tower 2, the oil is countercurrently contacted with solvent introduced into the top of tower Z through line 3. The solvent may suitably be wet furfural, that is, liquid furtural containing a small amount of dissolved water. Raiinatemix, comprising'retined light lubricating oil stock and a small amount of dissolved solvent is vwithdrawn through line 4 and passed to rafnate stripper 7. Water in the form of steam is introduced at the bottom of stripper 7 through line 8 in an amount suiiicient to form an azeotrope with all of the Solvent contained in the rainate-mix thereby removing all of the solvent in the azeotrope withdrawn as distillate through line 11i. Relined oil free of solvent is withdrawn from the bottom of stripper 7 through line 11.
The azeotropic mixture in line comprises vapors of solvent, water, and a small amount of hydrocarbon oil. The vapor mixture is condensed in cooler 15 and therresulting condensate is passed through line 16 to separator 17. Three liquid phases separate, that is an oil phase containing a small amount of dissolved solvent and water, a water phase containing a small amount of dissolved solvent and oil, and a solvent phase containing a small amount of water and oil. Separator 17 is provided with internal batlles indicated by dotted lines 1S and 19 to permit separate withdrawal of the three phases. Separated solvent phase is withdrawn through line 2@ and returned to extraction tower 2 through line 3. arated water phase is withdrawn through line 21 for subsequent solvent recovery. Separated oil phase is withdrawn through line 22, passed to washer 23 and countercurrently contacted with water therein introduced through line 24. Oil free of solvent is withdrawn through line 25 and combined with the rened oil in line 11 to provide a solvent reiined light lubricating oil stock product of the process. Water washings from washer 23 are withdrawn through line 26 and combined Sepwith the water phase in line 21 for subsequent solvent recovery. Y
Extract-mix comprising solvent and dissolved extracted oil is Withdrawn from the bottom of tower 2 through line 30. Extract-mix is cooled in cooler 31 land the cooled stream is passed through line 32 to settler 33. A secondary rarinate phase separates from the remaining extractmix in settler 33. This separated secondary ratinate contains a small amount of dissolved solvent and is withdrawn through line 36 and passed to wash tower 37 where it is countercurrently contacted with water intro- -duced through `line 33. Water washings are withdrawn through line 4t) for'subsequent solvent recovery. Washed secondary rainate is withdrawn through line 39 as a part ofV the extract product of the process discharged through line 41.
Secondary extract-mix withdrawn from settler 33 through line is heated in heater 46 and passed through line 47 to ash drum 48. In flash drum 43 all of the solvent is vaporized together with a part of the extracted hydrocarbon oil and the resulting vapors are discharged through line 49 to extractive distillation tower Sti. Stripped extract free of dissolved solvent is withdrawn from the bottom of tiash drum 4S through line 51 as a part of the extract product of the process discharged through line 41.
In extractive distillation tower 59, the hydrocarbon and solvent Yvaporsvare distilled in contact with a relat'ively high". boiling hydrocarbon oil introduced into the top of tower through line 5S. By distilling the solvent a-nd extract vapors in Contact with the high boiling oil, the extract vapors are condensed in the high boiling oil and solvent free of oil is removed as distillate through line 56. The extractive distillation tower bottoms, comprising the high boiling oil, extract oil, and a part of the solvent, are withdrawn through line 57 and passed to extract stripping tower 53.
Steam is introduced through line 59 into the bottom oftower 58 in an amount suicient to form the minimum boiling azeotrope with all of the solvent in the stream charged to tower 5S. All of the solvent is distilled overhead as azeotrope along with the extract oil. High boiling oil is withdrawn from the bottom of tower for recycle to extractive distillation tower 5t) through line 55. Extract and azeotrope vapors removed as distillate from tower 5S are passed through line 65, cooler and line 67 to separator 6%. Separator 6d is provided with internal battles indicated by dotted lines 69 and 7 ti to permit separation of the three liquid phases formed upon condensing the distillate from tower 53. VOil phase containing a small arount of dissolved water and solvent is withdrawn through line 72 and combined with the oil in line 36 for water washing and recovery. Separated water phase is withdrawn through line 71, combined with water streams in lines 21 and Alti and passed to fractionator 75 for recovery of dissolved solvent. Solvent phase is withdrawn through line`76 and recycled with the extract-mix in line 32 through the settler, flash drum and extractive distillation circuit.
Solvent vapors substantially free of oil in line 56 are condensed in cooler 77 and passed through line. 7S to water-solvent separator 79. Water phase separating in separator 79 is withdrawn through line 30 and passed to fractionator 75 for recovery of dissolved solvent. leparated solvent phase is passed through line S5 to accumulator Se from which solvent is withdrawn .through line 3 for charge to extraction tower 2.
Fractionator 75 is employed to recover solvent dissolved in water from the water discharged from the systent The Water streams charged through lines 21, 4t) and 3?, contain dissolved solvent which is removed by distilling the minimum boiling azeotrope overhead through line 87. The azeotrope vapor stream is combined with the vapor stream in line 56 for condensation, separation or solvent phase, and return to the extraction system. Water free of solvent is Withdrawn through line 8S for discharge from the system.
FGURE 2 illustrates a method of integrating the process of this invention into a system useful in the solvent refining of a full range of hydrocarbon oils including both oils containing solvent co-boiling components and oils wholly boiling substantially above the boiling range of the solvent. In the rening of high boiling hydrocarbon oils containing no components boiling in the region of the boiling range of the solvent, charge oil is introduced through line 101 into tower 102 and contacted countercurrently with solvent introduced through line 103. Raf. inate-mix withdrawn through line 105 is passed to rened oil stripper 1% where the solvent is removed by stripping with steam introduced through line 1417. Azeotropic mixture of steam and solvent is withdrawn through line 11@ for solvent recovery and reconcentration as will be described hereinafter. Rened oil is Vwithdrawn through line 111.
Extract-mix is withdrawn through line and passed to solvent iiash tower 121. The bulk of the solvent is removed as vapor free of oil through line 122 and passed to solvent drying tower 131 described hereinafter. Flashed extract-mix containing a small amount of residual solvent is passed through line 123 to stripper 124 wherein it is contacted with steam introduced through line 127 to remove residual solvent. An azeotropic mixture of solvent and water vapor is withdrawn through line for reconcentration and recovery. Extract free of solvent is withdrawn through line 126.
Solvent is recovered and concentrated in a distillation system comprising solvent recovery tower 130 and solvent solvent drying tower 131. In solvent drying tower 131, water is removedtrom the solvent by distilling all of the water overhead as the low boiling azeotrope which is discharged through line 31139 and combined with the azeotrope vapors in line 132 for condensation and phase separation. Solvent free of water is withdrawn from the bottom of tower 131 for recycle to extraction tower 102 through line .103.
Water phase from settler $5 is withdrawn through line 140 and passed to solvent recovery tower 130. In solvent recovery tower 130, all of the solvent is distilled overhead as the minimum boiling azeotrope which is discharged through line 141 and combined with the azeotropic mixture in line 132 for condensation and phase separation. Water free of solvent is discharged from the bottom of tower 13) through draw-oli line 141:1.
in reiining oils containing low boiling oils, both the raiiinate-mix in line 105 and the extract mix in line 120 may contain constituents co-boiling with the solvent. Low boiling constituents in the raiiinate-mix appear in the distillate from refined oil stripper 106, along with the azeotropic mixture of steam and solvent. This vapor mixture is withdrawn through line M and 11h11 to cooler 150. Condensed distillate is passed through line il to separator l52 whe-rein oil, water and solvent phases are separated. Oil phase is withdrawn through line 153 and passed to washer 155 wherein it is countercurrently contacted with water introduced through line 154. Light refined oil is discharged through line H6 and may be combined with the refined oil from line 111 as the reiined oil product of the process. Water washings are withdrawn from the bottom of tower 155 through line 166, combined with water phase withdrawn from separator 152, and the mixture passed through line 161 to solvent recovery tower 130.
Extract-mix containing constituents co-boiling with the solvent is withdrawn from tower 102 through line 125B and passed through line 12W to extractive distillation tower lofi Relatively high boiling oil is introduced to the top of tower 165 through line 166. Extract-mix is distilled in tower 16S under conditions effecting removal of the bulk of the solvent as an overhead distillate substantially free of hydrocarbon oil. Solvent vapor is discharged through line 167 and combined with the stream passed through line 125 for solvent recovery and concentration. Extractive distillation tower bottoms comprising a relatively small amount of solvent, the extract oil, and the relatively high boiling oil are withdrawn through line 170 and passed to tower 124.
Extractive distillation tower bottoms are distilled in tower i224 with steam introduced through line 127 under conditions etiecting vaporization and distillation of remaining solvent and extract oil which are discharged through lines 25 and 12551 to condenser 171. Condensed distillate is discharged through line 172 to separator 1173. Oil, Water and solvent phases are separated in separator 173. Oil phase is withdrawn through line 175 to washer 176 wherein it is countercurrently contacted with water introduced through line 177. Extract product of the process is discharged through line 178. Water washings are withdrawn from the bottom of washer 176 through line 179, combined with water phase withdrawn from separator 173 in line lh, and the mixture passed to solvent recovery tower 130. Separated solvent phase is withdrawn from separator 173 through line 190 and returned to the feed to extractive distillation tower in adniixture with the extract-mix in line 120g.
K Example The following example illustrates the application of the process of this invention to the reiining of a light lubricating oil stock useful in the manufacture of hydraulic oils. In the following example, ilow rates are expressed in terms of liquid barrels per hour regardless of whether the particular stream is in the liquid or vapor form. A lubricating oil charge stock having an ASTM distillation initial boiling point of 440 F., a 50 percent point of 490 F., and an endpoint of 632 F. at a rate of 18.7 barrels per hour is countercurrently contacted with 49.4 barrels per hour of solvent having a composition of 90 percent furfural, 9 percent water and 1 percent oil. Extraction is eected with a top tower temperature of 17l F. and a bottoni tower temperature of 122 F. Raiiinate-rnix at a rate of 15.3 barrels per hour is steam stripped at a top tower temperature of 208 F. to produce 12.7 barrels per hour of oil bottoms free of solvent and an overhead azeotropic distillate. The azeotropic distillate is condensed separating 1.7 barrels per hour of solvent phase comprising '86 percent furfural, 3 percent oil, and 1l percent water, 5.4 barrels of water phase comprising 92 percent water and 8 percent furfural and .4 barrel or" oil phase comprising percent oil, 18 percent furtural and 2 percent water. The solvent phase is returned as part of the solvent passed to the extraction tower, the water phase is directed to the solvent recovery equipment, and the oil phase is water washed and combined with the raiinate stripper bottoms to produce 13.0 barrels per hour of reiined oil product.
Extract-mix at a rate of 52.8 barrels per hour comprising 80 percent furfural, l2 percent extract oil, and S percent' water together with 4.8 barrels of recovered solvent as hereinafter provided comprising 75 percent turtural, 15 percent oil, and 10 percent water are cooled to 105 F. effecting separation of .5 barrel per hour ot secondary ratlinate which is water washed to provide a part of the extract product of the process. Remaining extract-mix is heated to 325 F. and dashed from a residue of 0.8 barrel per hour of extract. Flashed vapors equivalent to 56.2 barrels per hour are passed to an extractive distillation tower operated at atmospheric pressure and a top tower temperature of 325 F. A heavy paraliinic residual oil boiling wholly above 760 F. at atmospheric pressure is reiluxed to the top of the extractive distillation tower at a rate of 56.2 barrels per hour. Extractive distillation tower overhead at a rate of 46.2 barrels per hour comprising 89 percent furfural, 10 percent water and 1 percent oil is condensed and passed to a furfural-water settler.
Extract distillation tower bottoms, at a rate ot 66.2 barreis per hour comprising 8 percent extract, 7 percent furtural kand percent heavy oil is passed to an extract stripper. The extractive distillation tower bottoms are stripped with 12.7 barrels per hour or" steam at' a top tower temperature of 208 F. to separate 56.2 barrels per hour of heavy oil as bottoms for recycle to the extra/:tive distillation tower and 22.7 barrels per hour of distillate. Distillate is condensed to form oil-rich, water-rich and turfural-rich phases. Furfural phase at a rate of 4.8 barrels per hour comprising 75 percent furfural, l5 percent oil and l0 percent water is withdrawn and adrnixed with the extract-mix passed to the extractive distillation tower. Water at a rate of 13.2 barrels per hour containing 8 percent turfural is passed to a water from urfural fractionator for the recovery of furural. Oil phase at a rate of 4.7 barrels per hour is withdrawn, water washed, and combined with the secondary raffinate and the extract-mix ashed residue to produce 5.8 barrels per hour of extract product.
l claim:
l. ln the solvent refining of a feed hydrocarbon oil containing at least a small portion of constituents co-boiling with a liquid solvent wherein said feed hydrocarbon is contacted with said solvent in a solvent refining step forming separate extract and raiinate phases, said solvent being at least partially miscible with water at F. and capable of forming an azeotrope with water, the improvement' which comprises distilling at least a portion of said extract phase in contact with a relatively high boiling hydrocarbon oil consisting of hydrocarbons having true boiling points at least 100 F. above the boiling range of said solvent in an extractive distillation zone, withdrawing solvent free of co-boiling hydrocarbons as distillate from said extractive distillation Zone for recycle to said solvent refining step, passing bottoms from said extractive distillation zone comprising said relatively high boiling hydrocarbon oil, constituents of said feed co-boiling with said solvent, and solvent to an azeotropic distillation zone, passing steam to said azeotropic distillation zone, withdrawing said relatively high boiling hydrocarbon oil as bottoms from said azeotropic distillation zone for recycle to said extractive distillation zone, withdrawing ternary azeotrope comprising co-boiling oil, water, and solvent as distillate from said azeotropic distillation Zone, condensing said ternary azeotrope forming separate oil, water, and solvent phases, said separate oil phase comprising hydrocarbons coboiling with said solvent, withdrawing said separate oil phase, withdrawing said separate Water phase, recycling said separate solvent phase to said extractive distillation Zone, and recovering refined hydrocarbon oil from said ratiinate.
2. The process of claim l wherein said solvent cornprises furfural.
3. The process of claim 1 wherein said co-boiling hydrocarbons comprise hydrocarbons having true boiling points in the region of the solvent boiling temperature and below.
4. The process of claim 1 wherein said extractive distillation isV eected at an absolute pressure less than about rive atmospheres.
5. The process of claim 1 wherein tillation is effected under vacuum.
6. In the solvent refining of a feed hydrocarbon oil containing at least a small portion of constituents coboiling with a liquid solvent wherein said feed hydrocarbon is contacted with said solvent in a solvent refining step forming separate extract and raffinate phases, said solvent being at least partially miscible with water at 100 F. and capable of forming an azeotrope with water, the improvement which comprises distilling at least a portion of said extract phase in contact with a relatively high boiling hydrocarbon oil consisting of hydrocarbons having true boiling points at least 100 F. above the boiling range of said solvent in an extractive distillation zone, withdrawing solvent free of co-boiling hydrocarbons as distillate from said extractive distillation zone for recycle to said solvent refining step, passing bottoms from said extractive distillation zone comprising said relatively said extractive dishigh boiling hydrocarbon oil, constituents of said feed co-boiling with said solvent, and solvent to a first azeotropic distillation zone, passing steam to said first azeotropic distillation zone, withdrawing said relatively high boiling hydrocarbon oil as bottoms from said first azeotropic distillation Zone for recycle to said extractive distillation zone, withdrawing a first ternary azeotrope as distillate from said azeotropic distillation zone, condensing said first ternary azeotrope forming separate first oil, first water, and irst solvent phases, said first oil phase comprising hydrocarbons co-boiling with said solvent, withdrawing said first oil phase, withdrawing said first water phase, recycling said iirst solvent phase to said extractive distillation zone, passing said ratiinate phase to a second azeotropic distillation zone, passing steam to said second azeotropic distillation Zone, withdrawing refined hydrocarbon oil as bottoms from said second 'azeotropic distillation zone, withdrawing a second ternary azeotrope as distillate from said second azeotropic distillation zone, condensing said second ternary azeotrope forming separate second solvent, second oil, and second water phases, recycling said second solvent phase to said solvent refining step withdrawing said second water phase, Water washing said second oil phase, and withdrawing the water washed second oil phase.
7. The process of claim 1 wherein said extract phase is subjected to pre-distillation prior to passing to said extractive distillation Zone effecting separation of a portion of the extracted hydrocarbon oil free of solvent'.
References Cited in the file of this patent UNITED STATES PATENTS 2,216,932 Atkins Oct. 8, 1940 2,361,493 Patterson Oct. 31, 1944 2,526,722 Beavon Oct. 24,1950 2,567,172 Arnold et al. Sept. 11, 1951 2,685,556 Hachmuth Aug. 3, 1954 2,745,790 Manley May 15, 1956 2,842,484 Fleck July 8, 1958 2,908,731 Kohle Oct. 13, 1959 2,909,576 Penske et al. Oct. 20, 1959 2,936,283 Hutchings May 10, 1960 FOREIGN PATENTS 476,610 Great Britain Dec. 13, 1937

Claims (1)

1. IN THE SOLVENT REFINING OF A FEED HYDROCARBON OIL CONTAINING AT LEAST A SMALL PORITON OF CONSTITUENTS CO-BOILING WITH A LIQUID SOLVENT WHEREIN SAID FEED HYDROCARBON IS CONTACTED WITH SAID SOLVENT IN A SOLVENT REFINING STEP FORMING SEPARATE EXTRACT AND RAFFINATE PHASES, SAID SOLVENT BENING AT LEAST PARTIALLYU MISCIBLE WITH WATER AT 100*F. AND CAPABLE OF FROMING AN AZEOTROPE WITH WATER, THE IMPROVEMENT WHICH COMPRISES DISTILLING A TLEAST A PORTION OF SAID EXTRACT PHASE IN CONTACT WITH A RELATIVELY HIGH BOILING HYDROCARBON OIL CONSISTING OF HYDROCARBONS HAVING TRUE BOILING POINTS AT LEAST 100*F. ABOVE THE BOILING RANGE OF SAID SOLVENT IN AN EXTRACTIVE DISTILLATION ZONE, WITHDRAWING SOLVENT FREE OF CO-BOILING HYDROCARBONS AS DISTILLATE FROM SAID EXTRACTIVE DISTILLATION ZONE FOR RECYCLE TO SAID SOLVENT REFINING STEP, PASSING BOTTOMS FROM SAID EXTRACTIVE DISTILLATION ZONE COMPRISING SAID RELATIVELY HIGH BOILING HYDROCARBON OIL, CONSTITUENTS OF SAID FEED CO-BOILING WITH SAID SOLVENT, AND SOLVENT TO AN AZEOTROPIC DISTILLATION ZONE, PASSING STEAM TO SAID AZEOTROPIC DISTILLATION ZONE, WITHDRAWING SAID RELATIVELY HIGH BOILING HYDROCARBON OIL AS BOTTOMS FROM SAID AZEOTROPIC DISTILLATION ZONE FOR RECYCLE TO SAID EXTRACTIVE DISTILLATION ZONE, WITHDRAWING TERNARY AZEOTROPE COMPRISING CO-BOILING OIL, WATER, AND SOLVENT AS DISTILLATE FROM SAID AZEOTROPIC DISTILLATION ZONE, CONDENSING SAID TERNARY AZEOTROPE FORMING SEPARATE OIL, WATER, AND SOLVENT PHASES, SAID SEPARATE OIL PHASE COMPRISING HYDROCARBONS COBOILING WITH SAID SOLVENT, WITHDRAWING SAID SEPARATE OIL PHASE, WITHDRAWING SAID SEPARATE WAER PHASE, RECYCLING SAID SEPARATE SOLVENT PHASE TO SAID EXTRACTIVE DISTILLATION ZONE, AND RECOVERING REFINED HYDROCARBON OIL FROM SAID RAFFINATE.
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