US3511774A - Process for the demetallization of petroleum residuums - Google Patents

Process for the demetallization of petroleum residuums Download PDF

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US3511774A
US3511774A US700488A US3511774DA US3511774A US 3511774 A US3511774 A US 3511774A US 700488 A US700488 A US 700488A US 3511774D A US3511774D A US 3511774DA US 3511774 A US3511774 A US 3511774A
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solvent
metals
oil
supercritical
petroleum
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US700488A
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Robert B Long
Herman J Solomon
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G21/00Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003Solvent de-asphalting
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D11/00Solvent extraction
    • B01D11/04Solvent extraction of solutions which are liquid
    • B01D11/0403Solvent extraction of solutions which are liquid with a supercritical fluid
    • B01D11/0407Solvent extraction of solutions which are liquid with a supercritical fluid the supercritical fluid acting as solvent for the solute
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D11/00Solvent extraction
    • B01D11/04Solvent extraction of solutions which are liquid
    • B01D11/0488Flow sheets
    • DTEXTILES; PAPER
    • D01NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01HSPINNING OR TWISTING
    • D01H1/00Spinning or twisting machines in which the product is wound-up continuously
    • D01H1/14Details
    • D01H1/20Driving or stopping arrangements
    • D01H1/28Driving or stopping arrangements for two or more machine elements possessing different characteristics but in operative association
    • DTEXTILES; PAPER
    • D01NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01HSPINNING OR TWISTING
    • D01H4/00Open-end spinning machines or arrangements for imparting twist to independently moving fibres separated from slivers; Piecing arrangements therefor; Covering endless core threads with fibres by open-end spinning techniques
    • D01H4/42Control of driving or stopping

Definitions

  • Petroleum residuum fractions are demetallized in a multistage separation processcomprising conventional deasphalting followed by additional separation with a polar solvent at supercritical conditions.
  • organometallic compounds in petroleum fractions tend to poison petroleum refining catalysts employed in continuous operations. It is also well known that it is desirable to avoid high metal contents in fuel oils because metals cause corrosion and other problems when fuels are burned in industrial furnaces.
  • Certain petroleum residuum fractions have a metals content of over about 200 p.p.m.
  • Conventional propane deasphalting can be used to' separate an extract fraction containing about 5-100 p.p.m. metals which is a suitable material for treatment and conversion in the presence of catalysts.
  • propane deasphalting is limited in that 1twill extract only about 40-60% of a petroleum residuum and the bottoms fraction amounting to about ilal of] theresiduum is unsuitable for use except as heavy
  • the object of the process of this invention is to provide an additional quantity of oil having an intermediate quantity of metals that canA be used in a number of ways which will be described below.
  • the process comprises the steps of subjecting a residuum to conventional deasphalting, passing the asphalt to a supercritical separation unit, contacting the asphalt with a polar solvent atsupercritical conditions and recovering demetallized fractions.
  • a bottoms fraction or petroleum residuum having an initial boiling' "point in the range of 500-1000 F. islremoved by line 4 and passed to a conventional deasphalting tower 5.
  • the distillation bottoms can' be blended with other heavy fractions derived from petroleum refining operations.
  • the material will have av gravity of 525 API, a sulfur content of 1-8 wt. percent, a Conradson carbon of 5 25 wt. percent and a metals content of -2000 p.p.m.
  • the metals include vanadium, nickel, copper, iron and others.
  • Deasphalting is carried out in the conventional manner employing a non-polar light aliphatic hydrocarbon solvent containing 3 to 8 carbon atoms in the molecule.
  • propane, butane, pentane, hexane or mixtures thereof are used.
  • conditions in tower 5 include a temperature in the range'of 120 to F., a pressure in the range of 500 to 900 p.s.i.g. and a solvent to oil ratio of 0.5 to 8.0.
  • Deasphalted oil and solvent are passed overhead by line 6, cooled in cooler 7 and fed into ilash drum 8.
  • PropaneV is ilashed overhead and recycled via line 9, cooler 10 and pump 11 to tower 5.
  • This oil may be subjected to catalytic hydrodesulfurization since the metals content is now below the quantity of metals which causes rapid poisoning of hydrodesulfurization ⁇ catalysts such as cobalt molybdate on alumina.
  • the bottoms or raffinate from the deasphalter is passed by line 13 containing pump 14 to supercritical separation unit (SCS Unit) 15.
  • SCS Unit supercritical separation unit
  • a requirement of supercritical separation is that at least two phases must be formed by the solvent-feed mixture. If the properties of the feed are too similar to those of the solvent, the mutual solubility of thetwo will be so great that the formation of two phases will be impossible. Generally, it is preferred that the initial boiling point of the feed should be about 200 F. above the critical temperature of the solvent.
  • the mode of operation of supercritical separation and the processing equipment used are similar to those used in solvent extraction.
  • the solvent or carrier gas is mixed with the fraction or oil-solid slurry to be separated at supercritical conditions and two fluid phases are formed.
  • the feed and solvent are passed through a countercurrent contacting tower at supercritical conditions.
  • This unit may be either ⁇ single stage or multistage.
  • a light oil phase containing an intermediate quantity of metals is recovered overhead and a high metals asphalt phase is recovered as bottoms.
  • the solvent is recovered from the separated fractions and recycled.
  • the tower can have shed trays, rotating disc mixers, disc and donut trays, or the like as internals.
  • reilux may also be desirable.
  • the :paration may be carried out in a conventional mixerlttler type of contactor.
  • CT+ critical temperature plus
  • solvent or a carrier gas to extract a light l phase from an asphaltic feed is essentially nil at essures below the critical pressure of the solvent.
  • This pacrty increases with increasing pressure.
  • This operateI g pressure shall sometimes hereinafter be referred to as Pfl@ 1.e. critical pressure plus.
  • the optimum upper mt of operating pressure is not so sensitive or narrow terms of decline in selectivity as itis in the case of the per temperature limitation. Instead, equipment limitans such as wall thickness of reactors, separators and ning alect the selection of operating pressure.
  • the light phase taken overhead from the supercritical poration zone comprises a mixture of solvent and light at' supercritical conditions.
  • the oil can be recovered m the solvent by either increasing the temperature or decreasing the pressure on the light phase or both nultaneously. If desired, the light phase can be divided :o a multiplicity of fractions by stagewise alteration of nperature or pressure.
  • the supercritical solvent sometimes hereinafter referred as the carrier gas is a polar uid preferably a gas ving a critical temperature which is at least 200 F. s than that of the asphalt.
  • the polar solvent preferred is a nitrogen containing wis Base, an acid anhydride gas, acid gases such as 3l, HBr and HQS, or a low molecular weight organic lehyde, ether, alcohol, ketone or acid.
  • the critical aperties of some of the polar solvents are set forth Mixtures of any-of the above solvents can be used the polar components of the supercritical gas. Typical supercritical separation conditions for use with petroleum asphalt are set forth below in Table 1I.
  • dimethyl ether solvent is passed by line 16 into tower 15.
  • a light extract phase comprising oil having an intermediate metals content of about 1GO-500 p.p.m. and solvent is recovered overhead by line 17.
  • the light phase is passed through heater 18 into flash drum 19.
  • the solvent is dashed overhead into linel 16.
  • the solvent is cooled in coolerZt) and repressured by pump 21 for recycle to the SCS Unit.
  • Make-up solvent is added by line 22.
  • the intermediate metals oil is recovered by line 23.
  • a portion of the oil in line 23 is pumpedvia line 24 and pump 25 as reflux to the SCS Unit.
  • a portion of the oil is recycled by lines 23 and 26 to the inlet line 4 of the deasphalting tower for further treatment.
  • Another portion of the oil, i.e. 25-90% is recovered from the process byline 27. This oil is a suitable fuel oil.
  • High metals asphalt is recovered by line 28.
  • a process for the demetallization of a residuum fraction comprising the steps of (a) Contacting the residuum with a non-polar solvent at deasphalting conditions, l

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Spinning Or Twisting Of Yarns (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Braking Arrangements (AREA)

Description

M1t.)'l2,1970A Y R. a. LONG ETAL 3,511,774
' PROCESS FOR THE DEMETALLIZATION OF PETROLEUM RESIDUMS Filed Jan. 25. 1968 H. J. SOLOMON Inventors Patent Attorney i United States Patent O ice 3,511,774 PROCESS FOR THE DEMETALLIZATION OF i PETROLEUM RESIDUUMS ABSTRACT 0F THE DISCLOSURE A.process foil' the demetallization of a petroleum residuum fraction wherein the asphalt is contacted with a polar solvent at a (CT-l) of 5-50" F. above the critical temperature of the solvent and a (CP-|) pressure of 3D0-1000 p.s.i.g. above the critical pressure of the solvent.
Petroleum residuum fractions are demetallized in a multistage separation processcomprising conventional deasphalting followed by additional separation with a polar solvent at supercritical conditions.
v It. is well known that organometallic compounds in petroleum fractions tend to poison petroleum refining catalysts employed in continuous operations. It is also well known that it is desirable to avoid high metal contents in fuel oils because metals cause corrosion and other problems when fuels are burned in industrial furnaces.
Certain petroleum residuum fractions have a metals content of over about 200 p.p.m. Conventional propane deasphalting can be used to' separate an extract fraction containing about 5-100 p.p.m. metals which is a suitable material for treatment and conversion in the presence of catalysts. However, propane deasphalting is limited in that 1twill extract only about 40-60% of a petroleum residuum and the bottoms fraction amounting to about ilal of] theresiduum is unsuitable for use except as heavy The object of the process of this invention is to provide an additional quantity of oil having an intermediate quantity of metals that canA be used in a number of ways which will be described below. A
Briey summarizing, the process comprises the steps of subjecting a residuum to conventional deasphalting, passing the asphalt to a supercritical separation unit, contacting the asphalt with a polar solvent atsupercritical conditions and recovering demetallized fractions.
Further details of the invention will be disclosed with reference tov the drawing which discloses a preferred embodiment of the invention.
3,511,774 Patented May 12, 1970 Any number of fractions can be recovered from the distillation zone for further refining. A bottoms fraction or petroleum residuum having an initial boiling' "point in the range of 500-1000 F. islremoved by line 4 and passed to a conventional deasphalting tower 5. If desired, the distillation bottoms can' be blended with other heavy fractions derived from petroleum refining operations. Generally speaking, from 30-90% of the material in linev 4 boils above 900 F. The material will have av gravity of 525 API, a sulfur content of 1-8 wt. percent, a Conradson carbon of 5 25 wt. percent and a metals content of -2000 p.p.m. The metals include vanadium, nickel, copper, iron and others.
Deasphalting is carried out in the conventional manner employing a non-polar light aliphatic hydrocarbon solvent containing 3 to 8 carbon atoms in the molecule. Specifically, propane, butane, pentane, hexane or mixtures thereof are used. When propane is used-as the solvent, conditions in tower 5 include a temperature in the range'of 120 to F., a pressure in the range of 500 to 900 p.s.i.g. and a solvent to oil ratio of 0.5 to 8.0. Deasphalted oil and solvent are passed overhead by line 6, cooled in cooler 7 and fed into ilash drum 8. PropaneV is ilashed overhead and recycled via line 9, cooler 10 and pump 11 to tower 5. A low metals oil containing less than about 100 p.p.m. metals, preferably less than about 50 p.p.m. metals, is recovered `by line 12. This oil may be subjected to catalytic hydrodesulfurization since the metals content is now below the quantity of metals which causes rapid poisoning of hydrodesulfurization` catalysts such as cobalt molybdate on alumina.
The bottoms or raffinate from the deasphalter is passed by line 13 containing pump 14 to supercritical separation unit (SCS Unit) 15.
In supercritical separation, the separation of the fraction(s) is primarily by molecular weight of the components and this is similar to distillation. In addition some influences of compound type are evident resulting in separation effects like those of solvent extraction.
A requirement of supercritical separation is that at least two phases must be formed by the solvent-feed mixture. If the properties of the feed are too similar to those of the solvent, the mutual solubility of thetwo will be so great that the formation of two phases will be impossible. Generally, it is preferred that the initial boiling point of the feed should be about 200 F. above the critical temperature of the solvent.
The mode of operation of supercritical separation and the processing equipment used are similar to those used in solvent extraction. In one embodiment, the solvent or carrier gas is mixed with the fraction or oil-solid slurry to be separated at supercritical conditions and two fluid phases are formed. In a preferred embodiment shown in the drawings of this disclosure the feed and solvent are passed through a countercurrent contacting tower at supercritical conditions. This unit may be either `single stage or multistage. A light oil phase containing an intermediate quantity of metals is recovered overhead and a high metals asphalt phase is recovered as bottoms. The solvent is recovered from the separated fractions and recycled. The tower can have shed trays, rotating disc mixers, disc and donut trays, or the like as internals. In multistage peration, reilux may also be desirable. In addition, the :parationmay be carried out in a conventional mixerlttler type of contactor.
The most important operating variable in supercritical :paration is temperature. It is necessary to operate at a mperature signilcantly above the critical temperature the solvent in order to obtain the improved selectivity laracteristics of this process. This operating temperare shall sometimes hereinafter be referred to as CT+, e. critical temperature plus. For any particular feed ld solvent there isla narrow optimum CT+ range which illl provide the desired enhanced selectivity. If the opering temperature is below the optimum range, selectivity not improved. If thetemperature is above the optimum nge, the yield of the light phase is decreased. Pressure is also an important operating variable. The paclty of va. solvent or a carrier gas to extract a light l phase from an asphaltic feed is essentially nil at essures below the critical pressure of the solvent. This pacrty increases with increasing pressure. This operateI g pressure shall sometimes hereinafter be referred to as Pfl@ 1.e. critical pressure plus. The optimum upper mt of operating pressure is not so sensitive or narrow terms of decline in selectivity as itis in the case of the per temperature limitation. Instead, equipment limitans such as wall thickness of reactors, separators and ning alect the selection of operating pressure. The light phase taken overhead from the supercritical poration zone comprises a mixture of solvent and light at' supercritical conditions. The oil can be recovered m the solvent by either increasing the temperature or decreasing the pressure on the light phase or both nultaneously. If desired, the light phase can be divided :o a multiplicity of fractions by stagewise alteration of nperature or pressure. The supercritical solvent, sometimes hereinafter referred as the carrier gas is a polar uid preferably a gas ving a critical temperature which is at least 200 F. s than that of the asphalt. The polar solvent preferred is a nitrogen containing wis Base, an acid anhydride gas, acid gases such as 3l, HBr and HQS, or a low molecular weight organic lehyde, ether, alcohol, ketone or acid. The critical aperties of some of the polar solvents are set forth Mixtures of any-of the above solvents can be used the polar components of the supercritical gas. Typical supercritical separation conditions for use with petroleum asphalt are set forth below in Table 1I.
.una v11.--s'umtnonrfrrclsn SEPARATION CONDITIONS mperature Gradient, F
Referring to the drawing, dimethyl ether solvent is passed by line 16 into tower 15. A light extract phase comprising oil having an intermediate metals content of about 1GO-500 p.p.m. and solvent is recovered overhead by line 17. The light phase is passed through heater 18 into flash drum 19. The solvent is dashed overhead into linel 16. The solvent is cooled in coolerZt) and repressured by pump 21 for recycle to the SCS Unit. Make-up solvent is added by line 22. The intermediate metals oil is recovered by line 23. In a preferred embodiment a portion of the oil in line 23 is pumpedvia line 24 and pump 25 as reflux to the SCS Unit. In another preferred embodiment a portion of the oil is recycled by lines 23 and 26 to the inlet line 4 of the deasphalting tower for further treatment. Another portion of the oil, i.e. 25-90% is recovered from the process byline 27. This oil is a suitable fuel oil. High metals asphalt is recovered by line 28.
When the process of the invention is applied to typical Latin American feeds the following exemplary results will 4be obtained.
TABLE IIL-COMPOSITIONS AND YIELDS OR Table III. shows that only 10% of the crude oil is rejected as high metals asphalt. Supercritical separation thus provides an additional 1520% oil which can be blended with low metals oil, recycled to deasphaltingfor further metals reduction, or refined in suitable processes such as slurryhydro'desulfurization, coking, etc.
What is claimed is: i i
1. A process for the demetallization of a residuum fraction comprising the steps of (a) Contacting the residuum with a non-polar solvent at deasphalting conditions, l
(b) Recovering a low metals deasphalted oil extract,
(c) Contacting the asphalt with a polar solvent selected from the group consisting of ammonia, monomethyl amine, dimethyl amine, nitrous oxide, sulfur dioxide, methyl chloride, dimethyl ether, methyl alcohol, formaldehyde, acetone, HCl, -HBr and mixtures thereof at supercritical conditions in which the initial boiling point of the feed is about 200 F. above the critical temperature of the polar solvent,` and the pressure is above the critical pressure of the polar solvent, Y. A y
(d) Recovering an intermediate metalsextract of low` metals content, and f (e) Recovering a high'metals asphalt.
petroleum 2. Process according to claim 1 in whichsaid'residinrni'NV i fraction contains at least 100.p.p.m. metals; .L 3. A process for the'demetallization of a petroleum residuum fraction containing atleast p.p.m.metals" comprising the steps of (a) Countercurrently,contacting said lfeed in a `deasphalting zone with a process-solvent at a temperature inthe rangeof to 1959,11.,
(b) Recovering an extract phasev containing less than about 50 ppm. metals,
` 6 (c) Countercurrently contacting the raffinate from step 1 in a supercritical contacting zone with a polar References Cited solvent selected from the grdcltlilp t1coisisting ofularn- UNITED STATES PATENTS monia, monomethyl amine, e y amine, ni ous I oxide, sulfur dioxide, methyl chloride, dimethyl '5 afrsonal" ether, methyl alcohol, formaldehyde, acetone, HC1, 287g149 2/1959 a et 208 73 HBr and mixtures thereof at a (CI{) temperature ,2850 431 10/1958 s .n ""T' "208 "E09 of 5-50 F. above the critical temperature and a m1 (CP-H pressure of 30G-1000 p.s.i.g. above the FOREIGN PATENTS critical pressure, (d) Recovering an extract oil containing less than 500 1o 5661979 12/1958 Canada' p.p.m. metals, and (e) Blending the extract phases of steps 2 and 4. DELBERT E' GANTZ Primary Examiner 4. Process according to claim 3 in which the polar J- M- NELSON, Assistant EXamIler solvent is dimethyl ether. 15
5. Process according to claim 3 in which the polar U'S Cl' X-R- solvent is dimethyl amine. 208-86, 252, 309, 334
US700488A 1968-01-25 1968-01-25 Process for the demetallization of petroleum residuums Expired - Lifetime US3511774A (en)

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US3637483A (en) * 1969-11-10 1972-01-25 Ghenron Research Co Synthetic lubricating oil stock production
US3658695A (en) * 1970-12-14 1972-04-25 Phillips Petroleum Co Production of low-metal content gas oil from topped crude oil
US4035287A (en) * 1975-08-25 1977-07-12 Mobil Oil Corporation Desulfurization of residual oil
US4148716A (en) * 1977-10-21 1979-04-10 Gulf Research & Development Company Process for separating tar and solids from coal liquefaction products using a halogenated aliphatic solvent
EP0055627A1 (en) * 1980-12-31 1982-07-07 Exxon Research And Engineering Company Removal of metallic contaminants from petroleum fractions
US4354922A (en) * 1981-03-31 1982-10-19 Mobil Oil Corporation Processing of heavy hydrocarbon oils
US4354928A (en) * 1980-06-09 1982-10-19 Mobil Oil Corporation Supercritical selective extraction of hydrocarbons from asphaltic petroleum oils
US4363717A (en) * 1981-01-15 1982-12-14 Mobil Oil Corporation Conversion of heavy hydrocarbon oils
US4387016A (en) * 1980-11-10 1983-06-07 Gagon Hugh W Method for extraction of bituminous material
US4425225A (en) 1980-12-31 1984-01-10 Exxon Research And Engineering Co. Reducing metal content of oil feeds
US4446006A (en) * 1982-05-13 1984-05-01 Union Oil Company Of California Arsenic removal from hydrocarbons
US4465589A (en) * 1983-01-12 1984-08-14 Phillips Petroleum Company Removal of contaminants from organic compositions
US4502940A (en) * 1982-11-19 1985-03-05 Coal Industry (Patents) Limited Method for extracting caking coals
US4537676A (en) * 1980-12-31 1985-08-27 Exxon Research And Engineering Co. Reducing metal content of oil feeds
US4618413A (en) * 1985-07-15 1986-10-21 Exxon Research And Engineering Company Method for extracting nickel and vanadium compounds from oils
US4639273A (en) * 1983-05-06 1987-01-27 Morton Thiokol, Inc. Asphalt-adhesion improving additives prepared by formaldehyde condensation with polyamines
US4933067A (en) * 1988-11-01 1990-06-12 Mobil Oil Corporation Pipelineable syncrude (synthetic crude) from heavy oil
US5000838A (en) * 1989-12-13 1991-03-19 Mobil Oil Corporation Low efficiency deasphalting and catalytic cracking

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FR2096703B1 (en) * 1970-06-17 1973-10-19 Alsacienne Constr Meca
DE2058604B2 (en) * 1970-11-28 1977-08-25 Schubert & Salzer Maschinenfabrik Ag, 8070 Ingolstadt METHOD AND DEVICE FOR STOPPING AND STARTING UP AN OPEN-END SPINNING DEVICE
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DE2058602A1 (en) * 1970-11-28 1972-06-08 Schubert & Salzer Maschinen Control device for textile machines
DE2130690A1 (en) * 1971-06-21 1972-12-28 Skf Kugellagerfabriken Gmbh Method and device for re-spinning a broken thread in an open-end spinning device
CS164448B1 (en) * 1972-08-30 1975-11-07
DE2313788A1 (en) * 1973-03-20 1974-10-03 Krupp Gmbh PROCEDURE FOR INDEPENDENT START-UP AND STOP OF AN OPEN-END SPINNING MACHINE
CS176442B1 (en) * 1973-04-20 1977-06-30
USRE30167E (en) * 1973-04-30 1979-12-18 Apparatus and method for start-spinning on an open-end spinning machine
DE2321775C3 (en) * 1973-04-30 1979-07-05 Fritz 7341 Bad Ueberkingen Stahlecker Device for piecing which can be moved along an open-end spinning machine
JPS5059532A (en) * 1973-09-29 1975-05-22
DE2341528B2 (en) * 1973-08-16 1977-08-11 Stahlecker, Fritz, 7341 Bad Über kingen, Stahlecker, Hans, 7334 Süßen PROCESS FOR SPINNING A THREAD IN AN OPEN-END SPINNING UNIT
DE2351458C3 (en) * 1973-10-13 1977-10-06 Schubert & Salzer Maschinen DEVICE FOR THREAD ATTACHMENT ON AN OPEN-END SPINNING DEVICE
US4022011A (en) * 1974-02-13 1977-05-10 Hironori Hirai Yarn piecing method for open-end spinning machine
US4054024A (en) * 1974-09-30 1977-10-18 Hironori Hirai Apparatus for stopping and restarting the operation of an open-end spinning system
US4033107A (en) * 1975-05-22 1977-07-05 Kabushiki Kaisha Toyoda Jidoshokki Seisakusho Method and apparatus for controlling driving operation of open-end spinning frame
CS180952B1 (en) * 1975-10-07 1978-02-28 Marie Brozkova Apparatus for controlling spinning-in process in open-end rotor spinning machines
US4112661A (en) * 1977-04-15 1978-09-12 Kabushiki Kaisha Toyoda Jidoshokki Seisakusho Open-end spinning machine and a method of stopping the same
US4100722A (en) * 1977-04-18 1978-07-18 Kabushiki Kaisha Toyoda Jidoshokki Seisakusho Method of automatically piecing up a yarn in an open-end spinning machine and an open-end spinning machine for carrying out the same
US4163358A (en) * 1978-01-19 1979-08-07 Kabushiki Kaisha Toyoda Jidoshokki Seisakusho Apparatus for controlling the driving of an open-end spinning machine
US4159616A (en) * 1978-01-19 1979-07-03 Kabushiki Kaisha, Toyoda Jidoshokki Seisakusho Method for controlling an open-end spinning frame and an apparatus therefor
US4329839A (en) * 1980-04-14 1982-05-18 Vyzkumny Ustav Bavlnarsky Method of and apparatus for starting an open-end spinning machine
DE3526305A1 (en) * 1985-07-23 1987-01-29 Zinser Textilmaschinen Gmbh SPIDER
IT1227730B (en) * 1988-12-23 1991-05-06 Savio Spa PROCEDURE AND DEVICE FOR REFITTING THE THREAD WITH HIGH EFFICIENCY IN A FREE-END THREADING MACHINE
IT1227729B (en) * 1988-12-23 1991-05-06 Savio Spa PROCEDURE AND DEVICE FOR THE REMOVAL OF DETERIORATED FIBERS WHEN REFITTING THE THREAD IN AN OPEN-END THREADING MACHINE
CA2455011C (en) 2004-01-09 2011-04-05 Suncor Energy Inc. Bituminous froth inline steam injection processing

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US3637483A (en) * 1969-11-10 1972-01-25 Ghenron Research Co Synthetic lubricating oil stock production
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US4148716A (en) * 1977-10-21 1979-04-10 Gulf Research & Development Company Process for separating tar and solids from coal liquefaction products using a halogenated aliphatic solvent
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US4446006A (en) * 1982-05-13 1984-05-01 Union Oil Company Of California Arsenic removal from hydrocarbons
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Also Published As

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DE1911554A1 (en) 1970-01-15
FR2005800A1 (en) 1969-12-19
US3541774A (en) 1970-11-24
GB1253701A (en) 1971-11-17
CH485877A (en) 1970-02-15

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