US3200065A

US3200065A - Hydrocarbon treatment process

Info

Publication number: US3200065A
Application number: US124949A
Authority: US
Inventors: Gregory I Cottington
Original assignee: Texaco Inc
Current assignee: Texaco Inc
Priority date: 1961-07-18
Filing date: 1961-07-18
Publication date: 1965-08-10
Anticipated expiration: 1982-08-10

Description

G. l. COTTINGTON HYDROCARBON TREATMENT PROCESS kmh Aug. 10, 1965 United States Patent O "ice 3,200,065 HYDRCARBON TREATMENT PRCESS Gregory I. Cottington, Groves, Tex., assigner to Texaco Inc., New York, NX., a corporation of Delaware Filed July 18, 196i, Ser. No. 124,949 10 Claims. (Cl. 20d-321) 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 coboiling with the solvent. In accordance with the process of this invention, hydrocarbon oils containing constituents co-boiling with the solvent are contacted with a solvent in a liquid-liquid extraction zone forming separate primary extract and raiinate phases. The primary extract phase or a portion thereof is vaporized and contacted with a relatively high boiling hydrocarbon oil under vapor-liquid solvent extraction conditions effecting separation of solvent vapor free of co-boiling hydrocarbons from a secondary extract comprising said co-boiling hydrocarbon oil in solution with said relatively high boiling hydrocarbon oil. Said solvent vapor, free of co-boiling hydrocarbon oil, is condensed forming a purified solvent stream for recycle to said liquid-liquid extraction step.

In solvent refining processes wherein the solvent and material treated have substantially different boiling ranges, the solvent is readily separated from the extract and raffinate 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, although azeotropic distillation is etlected at a temperature substantially below the temperature of the boiling point of the pure solvent, substantial amounts of low boiling hydrocarbons may be vaporized with the azeotrope particularly when treating relatively low boiling stocks such as kerosene, diesel fuel, and hydraulic oils. In another prior art solution to this problem, the extracted oil is re-extracted from the solvent by liquid-liquid extraction with a relatively high boiling hydrocarbon oil. However, liquid-liquid extraction is only partially effective since in removing the co-boiling oils from the solvent, a portion of the high boiling oil dissolves in the liquid solvent. When solvent containing dissolved high boiling oil is returned to the primary extraction zone, the high boiling oil is transferred to the rafinate and contaminates the rened oil product. Although the dissolved high boiling oil can be removed from the solvent by distillation, this separation is costly since all of the solvent is removed as distillate from distilland comprising the dissolved high boiling oil.

In accordance with the process of this invention, at least a portion of the primary extract phase is extracted with a relatively high boiling hydrocarbon oil in vaporliquid extraction to effect a high degree of separation of co-boiling oils from the solvent. 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 kerosenes, diesel fuels, gas-oil cracking stocks, light 3,200,065 Patented Aug. l0, 1965 lubricating oil stocks, hydraulic oils, oils suited for the preparation of specialty products and oil suited for chemical manufacture. Although urfural is a preferred solvent useful in the process of this invention, other solvents may be employed particularly solvents which are partially miscible with Water at about F. and 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 mesityl oxide, hydroxy compounds, for example phenol and n-amyl alcohol, aldehydes, for example, benzaldehyde, nitriles, for example pripionitrile 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 modied by the inclusion of antisolvents, for example water.

In the vapor-liquid extraction step of this invention, separation of co-boiling hydrocarbons from the solvent in the primary extract is effected by vapor-liquid contact with a relatively high boiling hydrocarbon oil. Vaporliquid extraction conditions are maintained by effecting contact of the vapor and liquid at a temperature above the boiling point of the solvent. The extraction tower may be heated for example by applying heat directly to the top of the tower or by preheating the high boiling extraction oil fed to the top of the tower. The high boiling oil preferentially dissolves the co-boiling oil so that solvent vapors substantially free of co-boiling hydrocarbons are removed overhead and substantially all of the oil initially dissolved in the solvent is removed in solution in the relatively high boiling oil as secondary extract. The relatively high boiling oil itself should be free of cornponents boiling in the region of the solvent and preferably should consist of components having true boiling points at least 100 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 co-boiling oil in which case the boiling range of the two oils, that is the hydrocarbon oil feed and the relatively high boiling hydrocarbon oil, 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 oil should consist of components boiling wholly above the hydrocarbon oil feed. Suitable high boiling oils include both distillates and residua. A parallinic residuum boiling wholly above 760 F. at atmospheric pressure is preferred for use as a relatively high boiling oil when treating hydrocarbon oil feeds 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 co-boiling 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 of the solvent.

The accompanying llow diagram illustrates the process of this invention. Although the drawing illustrates one mode of practicing this invention, it is not intended to limit the invention to the particular apparatus or materials described.

Referring to the ligure, a light lubricating oil stock is charged through line 1 to extraction tower 2. In extraction tower 2, the oil is countercurrently contacted with solvent introduced into the top of tower 2 through line 3. The solvent may suitably be wet furfural, that is, liquid furfural containing a small amount of dissolved water. Rafnate-mix, comprising refined light lubricating oil stock and a small amount of dissolved solvent is withdrawn through line 4 and passed to raflinate stripper 7. Water in the form oi' steam is introduced at the bottom of stripper '7 through line 8 in an amount sutlicient to form an azeotrope with all of the solvent contained in the raflinate-mix thereby removing all of the solvent in the azeotrope withdrawn as distillate through line l0. Relined oil free of solvent is withdrawn from the bottom of stripper 7 through line 11.

The azeotropic mixture in line tu comprises vapors of solvent, water, and a smallV amount of hydrocarbon oil.

The vapor mixture is condensed in cooler and the resulting condensate is passed through line i6 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 battles indicated by dotted lines i8 and l@ to permit separate withdrawal of the three phases. Separated solvent phase is withdrawn through line 2t? and returned to extraction tower 2 through line 3. Separated water phase is withdrawn through line 2li 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 reiined oil in line lll to provide the solvent refined light lubricating oil stock product of the process. Water Washings from washer 23 are withdrawn through line 2o and combined with the water phase in line 21 for subsequent solvent recovery.

Primary extract-mix comprising solvent and dissolved extracted oil is withdrawn from the bottom of tower 2 through line 30. Primary extract-mix is heated in heater 3l to a temperature substantially above the boiling point of the solvent to vaporize all of the solvent and a portion of the oil dissolved therein. The resulting vapor-liquid mixture is passed through line 32 to primary extract stripper 33. Stripper 33 is employed as a prefractionator and may be operated as a simple flash tower or may be provided with reboiler heat and reflux by conventional means not shown. Stripper 33 is operated to separate solvent containing co-boiling hydrocarbons as distillate from a bottoms product free of solvent. Bottoms from stripper 33 are withdrawn through line 34 as a part of the extract product of the process. Solvent Vapor together with coboiling hydrocarbon oil vapor is discharged from extract stripper 33 through line 49 to vapor-liquid extraction tower 59. Extraction tower dil may be for example, a packed tower, a bubble tower, or other means known in the art for electing vapor-liquid Contact. ing a high length to diameter ratio is preferred. Contacting may be effected in a single stage or in niultistages and on a continuous or batch basis. In extraction tower 50, the co-boiling hydrocarbon and solvent vapors are countercurrently contactedwith a relatively high boiling hydrocarbon oil introduced into the top of tower S@ through line 55 at a temperature above the boiling pointV of the solvent. By contacting the solvent and co-boiling extract vapors with 'the liquid high boiling oil, the co-boiling oil vapors are condensed in the high boiling oil and solvent vapors free of oil are removed through line 5o. A secondary extract comprising the high boiling oil, extracted co-boiling oil, and a small amount of dissolved solvent, is withdrawn through line 57 and passed to secondary extract stripping tower S8.

Steam is introduced through line 59 into the bottom of tower 58 in an amount suiicient to form the minimum boiling azeotrope with all of the solvent in the secondary A. tower havaandoen g extract. All of thesolvent is distilled overhead as azeorope along with .the co-boiling extract oil; Y High boiling oil is withdrawn from the bottom of tower 58 for recycle Lto vapor-liquid extractive distillation tower through line 5S. Co-boiling oiland azeotrope vapors removed as distillate from tower :58 are passed through line 65, cooler 66 and line 67 to separator 68. Separator 68 is provided with internal bafes indicated by

dotted lines

69 and 78 to permit separation ot the three liquid phases formed upon condensing the distillate from tower 58. Oil phase `containing a small amount of dissolved water'and solvent is withdrawn through line 72 and passed to extract washer 73. ln washer 73 the oil is countcrcurrently contacted with water introduced through line 7,4. .Water washings are withdrawn for solvent'recovery through line 75 and washed oil is withdrawn through line 76 and combined with the extract oil product in line 34e. Separated water phase is withdrawn from separator 68 through line 7l, combined with water streams in line 21 and '75 and passed to fractionator 77 for recovery of dissolved solvent. Solvent phase is withdrawn through line 78 and recycled with the primary extract-mix in line 3@ for solvent recovery. v v

Solvent vapo-rs substantially free of oil in line 56 are condensed in cooler 8d and passed through line 81 to water-solvent settler 82. Water phase separating in settler 82 is withdrawn through line 83 and passed to fractionator .77 for recovery of dissolved solvent. 'Separated solvent phase is withdrawn from settler S2 through line 3 for charge to extraction tower 2. y Y

A Fractionator 77 is employed to` recover solvent dissolved in water from the water discharged from the system. The water stream charged through lines 21, 26, '71, 75 and 83 contain dissolved sol'ventwhich is removed by distilling the minimum boiling azeotrope overhead through line 87. The azeotrope vaporstream is combined ywith the vapor-stream in line S5 for condensation, separation of solvent phase, and return to the extraction system. Water free of solvent is withdrawn through line 88 for discharge from the system.

Example The fohowing example illustrates the application of the process of this invention to the refining of 1a light lubricating oil stoel; useful in the manufacture of hydraulic oils. ln the following example, ilow rates are expressed in terms or" liquid barrels per hour regardless of whether the particular-stream is in the liquid or vapor form. Y i

A lubricating oil charge stock having a gravity of 30.9 APL lan ASTM distillation initial boiling point of 440 F., a 50 percentY point of 490 F., and an endpoint of 632 F. Vat a rate of l) barrels per hour is countercurrently contacted with 263 barrels per .hour of solvent having a cornposition of 90 percent furtural, 9 percent water and l percent oil in a primary extraction tower. Extract-ion is eiected with a top tower temperature of 171 E.' and a bottom tower temperature of V122 F. to produce 82 barrels per hour of ratlinate mix and 281 barrels per hour of primary extract rnix. Refined oil product at a rate of 69 barrels per hour is separated from the ratlinate-mix for hydrauiic oil manufacture. Y

Primary extract-mix at a rate of 281 barrels per hour comprising percent furfural l2 percent extract oil, and 8 percent Water together with 15 barrels per hour of recovered solvent as hereinafter provided comprising 75 percent furfural, l5 percent oil and lpercentwater are prefractionated effecting separation of 14 barrels per hour of stripped extract and 282 barrels per hour of overhead vapor. This overhead vapor includes all oi the furfural and water and 58.3 percent of the oil in the prefractionator feed. This overhead vapor is passed to a vapor-liquid extraction tower operated at a top tower temperature of 380 F. A heavy paraiiinic residual oilboiling wholly above 760 F. at atmospheric pressure is fed to the top of the extraction tower at a rate of 350 barrels per hour.

Overhead vapor from the extraction tower is condensed to produce 253 barrels per hour of recovered solvent comprising 90 percent furtural, 9 percent water and 1 percent oil for recycle to the primary extractio-n tower.

Secondary extract-mix, :at a rate of 379 barrels per hour comprising 6 percent extracted oil, 3 percent furfural and 91 percent heavy oil is withdrawn from the bottom of the vapor-liquid extraction tower.

Secondary extract-mix is stripped with steam to separate a bottoms fraction of heavy oil at a rate of 350 barrels per hour which is recycled to said vapor-liquid extraction tower. Secondary extractmix stripper overhead is condensed forming oil, water, and furtural rich phases. An additional 16 barrels per hour of extract product is separated by water washing the oil. The furfural rich phase at a rate of barrels per hour is recycled as said recovered solvent in admixture with said primary extract mix. Remaining furfural is recovered from solution in the collected water steams by azeotropc distillation.

I claim:

1. in the solvent reiining 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 liquid-liquid extraction Zone forming separate primary extract and rafiinate phases, the improvement which comprises vaporizing at least a portion of said primary extract phase forming `a vapor comprising solvent and co-boiling hydrocarbon oil, contacting said vapor with liquid comprising 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 a vapor-liquid extraction Zone, withdrawing solvent vapors free of coboilng hydrocarbons as overhead vapor from said vaporliquid extraction Zone, condensing said overhead vapor forming a puried solvent stream for recycle to said solvent refining step, and withdrawing secondary extract comprising said relatively high boiling hydrocarbon oil and said co-boiling hydrocarbon oil from said vaporliquid extraction zone.

2. The process of claim 1 wherein said solvent is at least partially miscible with water at 100 F. and is capable of forming an azeotrope with water.

3. The process of claim l wherein said relatively high boiling hydrocarbon oil consists of hydrocarbons boiling above the boiling range of said co-boiling hydrocarbon oil.

4. The process of claim 3 wherein ysaid secondary extract is distilled separating said co-boiling hydrocarbon oil as overhead and said relatively high boiling hydrocarbon oil as bottoms for recycle to said vapor-liquid extraction Zone.

5. The process of lclaim 2 wherein said secondary extract comprises solvent, said relatively high boiling hydrocarbon oil, and said co-boiling hydrocarbon oil, and said secondary extract is distilled in the presence of steam effecting separation of said co-boiling hydrocarbons and lazeotrope of solvent and water as distillate and said relatively high boilinghydrocarbon oil as bottoms for recycle to said vapor-liquid extraction Zone.

6. The process of claim 5 wherein said distillate is condensed forming separate oil, water, and `solvent phases, ico-boiling hydrocarbon oil is recovered from said oil phase, and said solvent phase is combined with said primary extract.

7. The process of claim 1 wherein said primary extract is prefractionated prior to said vapor-liquid extraction effecting separation of said vapor comprising solvent and co-boiling hydrocarbons, and distilland comprising extracted hydrocarbon oil free of solvent is withdrawn as prefractionator bottoms.

8. The process of claim 1 wherein said solvent comprises furfural.

9. The process of claim 1 wherein said ico-boiling hydrocarbons comprise hydrocarbons having true boiling points inthe region of the solvent boiling temperature and below.

10. The process oi claim 8 wherein said relatively high boiling hydrocarbon oil comprises a paratnic oil having an ASTM distillation initial boiling point of at least 625 F.

References Cited by the Examiner UNITED STATES PATENTS Atkins 208-316 ALPHONSO D. SULLIVAN, Primary Examiner.y

Claims

1. 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 LIQUID-LIQUID EXTRACTION ZONE FORMING SEPARATE PRIMARY EXTRACT AND RAFFINATE PHASES, THE IMPROVEMENT WHICH COMPRISES VAPORIZING AT LEAST A PORTION OF SAID PRIMARY EXTRACT PHASE FORMING A VAPOR COMPRISING SOLVENT AND CO-BOILONG HYDROCARBON OIL, CONTACTING SAID VAPOR WITH LIQUID COMPRISING A RELATIVELY HIGH BOILING HYDROCARBON OIL CONSISTING OF A REALTIVELY HIGH BOILING HYDROCARBON OIL CONSISTING OF HYDROCARBINS HAVING TRUE BOILING POINTS AT LEAST 100*F. ABOVE THE BOIL RANGE OF SAID SOLVENT IN A VAPOR-LIQUID EXTRACTION ZONE, WITHDRAWING SOLVENT VAPORS FREE OF COBOILING HYDROCARBONS AS OVERHEAD VAPOR FROM SAID VAPORLIQUID EXTRACTION ZONE, CONDENSING SAID OVERHEAD VAPOR FORMING A PURIFIED SOLVENT STEAM FOR RECYCLE TO SAID SOLVENT REFINING STEP, AND WITHDRAWING SECONDARY EXTRACT COMPRISING SAID RELATIVELY HIGH BOILING HYDROCARBON OIL AND SAID CO-BOILING HYDROCARBON OIL FROM SAID VAPORLIQUID EXTRACTION ZONE.