• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
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    • 专利摘要:
    A continuous solvent extraction process for tar-sand uses a closed rotary contactor. A tar-sand/water slurry stream and a solvent stream are passed countercurrent through the contactor and three phases are formed: tar-sand solids at the bottom of the contactor, a barrier layer of water in which the solids are contained and an uppermost solvent phase. The solids during their travel through the contactor are repeatedly lifted off the bottom of the contactor and tumbled through the solvent phase so that the bitumen oils content of the tar-sand is progressively dissolved in the solvent. A solvent stream containing the dissolved bitumen oils is removed from one end of the contactor and discard stream consisting essentially of sand and water is removed from the other end.
    公开号:SU959629A3
    申请号:SU772510551
    申请日:1977-08-05
    公开日:1982-09-15
    发明作者:Сатиапракаш Рендалл Джон
    申请人:Ртл Контэктор Холдинг Са (Фирма)；
    IPC主号:
    专利说明:

    (5) METHOD FOR OBTAINING BITUMEN OILS FROM BITUMINOUS SANDLER
    The invention relates to methods for producing bituminous oils from tar sands and can be used in the oil industry .5
    A method is known for producing bituminous oils from tar sands by extraction using f1J solvents.
    The closest to the invention is a method of obtaining bituminous oils from tar sands by extraction using a hydrocarbon solvent, which has a density less than water and water 15 to obtain an extract.}.
    However, this method is not sufficiently effective due to the need to mix the initial tar sands with a large amount of 20 L dissolving, which requires a large amount of energy for mixing the suspension with a mixer having a speed of 25QO rpm. In the future, water is added to the resulting suspension. extract and raffinate c. the subsequent separation of the extract into the desired product and solvent and the return of the latter to the extraction.
    The aim of the invention is to increase the efficiency of the process by reducing the amount of solvent used and simplifying the process technology.
    The goal is achieved in that, according to the method for producing bituminous oils from tar sands, the raw material is mixed with water to produce sludge and extraction is carried out in a closed horizontal contact apparatus containing a drum with scoops rotating around a horizontal axis. at the entrance to the apparatus 20-95 C and the solvent flow with the formation in the apparatus of the liquid phases of the hydrocarbon solvent and water and the phase of solid particles of bituminous sandstone, and the water phase forms a barrier layer between the 39596 solvent phase and the solid particle phase, with simultaneous multiple washing of the solid particles through the liquid phases in the contact apparatus, followed by extracting the extract from the upper part of the apparatus, and from the lower part of its stream of washed solid particles and water, and further separation of the latter and return it to mix with the raw materials. The amount of water added to the feedstock is determined by the possibility of pumping bituminous sandstone sludge and water into the contact apparatus as well as the need for free movement of the bituminous sandstone and water through the contact apparatus and the necessity of surrounding the sand in the contact apparatus with water to prevent the solvent from contacting the water. The amount of water is at least 20 wt.%, Preferably more than 0% and most preferably more than 50 wt.. Since the density of the solvent in the solvent stream is less than the density of water and the solvent does not mix with water, water and solvent form two separate phases, and any solvent Adhering to the solid particles during the washing through the contact apparatus, quickly returns to the solvent phase. The amount of solvent used depends on the nature of the bituminous sandstone and is 10-85% by weight, preferably 20-80 by weight of the bituminous oils in the bituminous sandstone. The solvent used is a hydrocarbon oil or a mixture of oils. The most effective solvent has a kerosene boiling range (200-295 ° C). A fraction of extracted bituminous oils with a similar boiling range can also be used as a solvent. Usually, a stream of solvent withdrawn from the contact apparatus with the bituminous oils dissolved in it is fed to an installation for extracting a solvent, from which the extracted solvent is recycled to the contact apparatus; . A solution of bituminous oils in a solvent can be passed through an oil refinery to produce a product that can be used as a solvent. 9 The temperature of the sludge fed to the contact apparatus is 20-95 0 preferably 50-75 C. In FIG. 1 shows a flow chart for carrying out the proposed method; in fig. 2 tons of contact apparatus, radial section; in fig. 3 technological scheme, in which the fractionation column is replaced by oil refining equipment. . The method is carried out as follows. Ground tar sands (Fig. 1) are fed along line 1 to a rotating one. autoclave 2, where it is mixed with hot water sent through line 3 from the hot water tank. Recycled water from tank C is supplied by pump 5 through fuel heater 6 so that the water temperature at the inlet to autoclave 2 is. l / ebs. If necessary, steam can be supplied to autoclave 2 via line 7. Bituminous sandstone slurry in water from autoclave 2 is sent through stripping sieve 8 to pressure tank 9 where hot water is added along line 3 as needed to bring the slurry temperature to, lh b5 C and to maintain solid particles in suspension. Hot sludge (tar sand and water) is fed by pump 10 from tank 23 to a contact device, with the sludge being directed to the bottom of the contact device. Hot sludge fed into the contact apparatus as a stream from one end of the contact apparatus gradually passes all the compartments of the contact apparatus through the annular gaps and is discharged through line 14. Hydrocarbon solvent will sweep across the top 15 of the contact apparatus and output along the line 1b from the top of the contact device. The solvent is pumped by pump 17 from the solvent storage tank 18. The solvent can be heated using a steam preheater 19 before it is fed to the contact apparatus. A stream of solvent that does not actually mix with water forms a distinct, separated phase above the feed stream of sludge. The contact device operates in such a way that the interface between the two phases remains static and is located near the axis (horizontal) of the contact device.
    Thus, bituminous oils gradually dissolve in the solvent stream and the "flow of sand and fine particles gradually separates from the bituminous oils. ,
    The contents of the contact apparatus form three phases: the bottom - the sand, which quickly settles on the bottom of the contact apparatus, the middle layer - the water in which there is sand, and the upper layer - the solvent. The presence of water surrounding the sand plays an important role in the formation of a barrier separating the solvent from the sand, and causes the rapid removal of any solvent from the sand trapped. Because of this, by the time the sand moves to the outlet end of the contact apparatus, there is little or no solvent left in the sand. The flow discharged through line T consists almost entirely of water, sand and fine particles, and the solvent flow produced through line 16 consists almost entirely of a solution of bituminous oils extracted in a solvent. The extraction process that takes place in the contact apparatus is thus continuous, countercurrent and. 1 multistage. From the contact apparatus, the flow of the bituminous oils is sent along line 16 to the storage tank 21, from which the pump 22 through the heat exchanger 23 feeds it to the heater 2, which runs on gas or fuel oil. The solution heated to temperature f is fed to the fractionation column 25. The vapors discharged from the top of the column are fed to pi 26 on the condenser 27. Condensate of water and light oils is directed to tank 28, while water from the bottom layer is recirculated along the line to tank 7. Light the upper layer oils are sent to the storage tank 30 and some of them are pumped via line 31 to the column 25 as a reflux, the remainder is sent to the bitumen oil tank 23, which is pumped to the oil refinery (not shown in Fig. 1) . A fraction with a kerosene boiling range, for example, 200-295C, is taken from column 25 as a side stream and fed to a stripping section 33, into the base of which a steam is introduced along line 3. The resulting solvent fraction is cooled in a refrigerator 35
    to temperature / in solvent storage tank 18. Fresh solvent is supplied to tank 18 through the ST lines. The product from the bottom of the column is a 25-high-boiling bitumen oil — withdrawn from the bottom of the column and, after cooling in a heat exchanger 23, is pumped through a cooler 37 into a tank, 32 for storing bituminous oils. Warm cooling water from cooler 37 as well as from heat exchangers. 19, 35 and 27 is fed through line 29 to a hot water tank.
    The solvent fraction obtained from the fractionation column 25 and recovered in the stripping section 33, co. holds not only the solvent, but also fraction (and bituminous oils contained in tar sands and having the same boiling point range. Thus, this system is self-sufficient in solvent, and the solvent is supplied from an external source only at start-up. The solvent extraction system I works at atmospheric pressure or at a pressure below atmospheric. I The flow discharged from the contact apparatus, along line 1, is directed to a sand cleaning unit; The sand cleaning unit is a conical closed sepa Ator 38. The incoming stream passes through section 39 enclosed in a nozzle, which is designed to eliminate surface water turbulence in the upper part of the separator. Heavier sand quickly settles at the base of the separator, and fine water enters section 39 further in the same; 0. The steam is supplied to the base of the separator via the At line, which is closed by the valve outlet 42. The steam performs two functions: it maintains free flow of sand coming from the separator and helps to remove any dissolved solvent that ozhet present in the water. The vapor along with the solvent vapor is removed from the top of the separator 38 and condensed in the condenser 3, while the hot condensate is directed to the hot water tank along with the warm cooling water. Steam from separator 38 can be condensed in an irrigation condenser. Water particles from separator 38 are directed along chute 0 into a centrifugal separator, which concentrates the fine particles into sludge mixed with sand coming from the valve outlet k2. Water that is free of fine particles, leave the centrifugal separator kk and return to tank i-for hot water through line 5.
    The flow of sand, fine particles and water from the separator 38 is diverted along the line k6.
    Bituminous sandstone and water are continuously treated in each compartment of the contact apparatus with rotating kj and kB scoops. At the same time, solids are raised with scoops and gradually discharged from the scoops in the upper half of the body kS so that they are treated in a barban or washed with solvent 50. Since the solid particles are denser than water or solvent, they, when unloaded from the scoops, quickly pass through a stream of solvent and settle to the bottom of the apparatus. The rotating scoops also transfer down the solvent from stream k to stream 51 of tar sand and water, and the solvent is there in the form of droplets, which quickly return upwards to the stream of solvent,
    The leading edges of the scoops kf and 8 are perpendicular to the gap between the disk 52 and the housing 9.
    In the flow chart depicted in FIG. 3, the fractionation column, which serves to isolate the hydrocarbon solution of the bodies, replacing ia by refining with the installation 53 Raw materials for it - a solution of bituminous oils are directed along line 5.
    The hydrocarbon solvent obtained in the plant can be subjected to various treatments, such as hydrocracking, for quality improvement. The hydrocarbon solvent is removed from the refinery and introduced to the process via line 55.
    In tab. 1 and 2 show the material balance and the conditions of the processes, respectively, according to the diagrams shown in FIG. 1 and 3.
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    rf 19 of the invention. A method for producing bituminous oils from bituminous sandstones by extraction using a hydrocarbon solvent having a density less than water and water to obtain an extract is about the fact that, in order to increase the efficiency of the process, the feedstock is mixed with water to produce sludge and the extraction is carried out in a horizontally closed contact apparatus containing a drum rotating around a horizontal axis with scoops by passing through it a countercurrent sludge with temperature Atura at the inlet of the apparatus and the solvent flow to form in the apparatus the liquid phases of the hydrocarbon solvent yt of water and the phase of solid particles of bituminous sandstone, and the water phase forms a barrier joint between the solvent phase and the phase of solid particles, with simultaneous repeated washing of solid particles through the liquid phases at. contact apparatus with the last (food 920 extract output from the upper part of the apparatus, and from the bottom of its stream washed solids and water, separation of the latter and return to mixing with the feedstock. The priority is 07.08.76 - countercurrent sludge and solvent flow; use hydrocarbon solvent;, use of a closed horizontal contact apparatus containing a rotating around the horizontal axis of the barrel with scoops. 25.01.77 - the temperature of the slurry at the entrance to the apparatus is 20-95 0; about the solvent from the extract and returning it to extraction; returning to mixing with the feedstock Sources of information taken into account in examination i 1. US Patent No. 3558469, L. 208-11, published 1971. 2. US Patent No. 3553098 , Cl. 208-11, published 197 (prototype).
    50
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    权利要求:
    Claims (1)
    [1]
    Claim
    A method for producing bituminous oils from tar sandstones by extraction using a hydrocarbon solvent having a density lower than water and water to obtain an extract is based on the fact that, in order to increase the efficiency of the process, the initial raw materials 10 are mixed with water to obtain sludge and extraction is carried out in a closed horizontal contact apparatus containing a drum with scoops rotating around a horizontal axis, by passing 15 through it a countercurrent sludge with a temperature at the inlet to the apparatus t 20-9J C and a solvent stream with the formation in the apparatus of liquid phases of a hydrocarbon solvent and water 20 and a phase of solid particles of tar sandstone, wherein the water phase forms a barrier layer between the phase of the solvent and the phase of solid particles, with simultaneous multiple 25 washing of solid particles through the liquid phases c. contact apparatus with the subsequent withdrawal of the extract from the upper part of the apparatus, and from the lower part of its flow of washed solid particles and water, separation of the latter and return to mixing with the feedstock.
    Priority but featured
    O7.O8.76 - counterflow of sludge and solvent stream; the use of a hydrocarbon solvent ;, the use of a closed horizontal contact apparatus comprising a drum with scoops rotating around a horizontal axis.
    01/25/77 the temperature of the sludge at the entrance to the apparatus, equal to 20-95 * 0; the selection of a hydrocarbon solvent from the extract and returning it to extraction; return of thieves to mixing with the feedstock.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU959629A3|1982-09-15|Process for producing bitumen oils from bitumenous sandstones
    US5236577A|1993-08-17|Process for separation of hydrocarbon from tar sands froth
    US5534136A|1996-07-09|Method and apparatus for the solvent extraction of oil from bitumen containing tar sand
    US4875998A|1989-10-24|Hot water bitumen extraction process
    US4514305A|1985-04-30|Azeotropic dehydration process for treating bituminous froth
    US6358403B1|2002-03-19|Process for recovery of hydrocarbon from tailings
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    US4424112A|1984-01-03|Method and apparatus for solvent extraction
    US8658029B2|2014-02-25|Dry, stackable tailings and methods for producing the same
    US4120775A|1978-10-17|Process and apparatus for separating coarse sand particles and recovering bitumen from tar sands
    US4722782A|1988-02-02|Method for solvent treating of tar sands with water displacement
    US3875046A|1975-04-01|Recovery of oil from tar sand by an improved extraction process
    US3684699A|1972-08-15|Process for recovering oil from tar-oil froths and other heavy oil-water emulsions
    CA2712725C|2012-11-27|Apparatus and method for recovering a hydrocarbon diluent from tailings
    CA1267860A|1990-04-17|Inclined plate settling of diluted bitumen froth
    US3161581A|1964-12-15|Centrifugal processing of tar sands
    CA2021185C|1998-09-15|Process for separation of hydrocarbon from tar sands froth
    GB2044796A|1980-10-22|Extraction of bitumen from oil sands
    US4422901A|1983-12-27|Apparatus for the continuous solvent extraction of bitumen from oil-bearing sand
    US4396498A|1983-08-02|Treatment of heterogeneous liquid materials
    US3117922A|1964-01-14|Recovery of bitumen from bituminous sand
    US3711400A|1973-01-16|Continuous process for recovering waxes from oily sludges
    US2914455A|1959-11-24|keller
    US1904521A|1933-04-18|Separation of oils from solid residues
    CA2969872C|2020-02-25|Recovery of hydrocarbon diluent from tailings
    同族专利:
    公开号 | 公开日
    CA1085763A|1980-09-16|
    US4160718A|1979-07-10|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1520752A|1920-02-27|1924-12-30|Horwitz Wilhelm|Process for the recovery of petroleum|
    US1487541A|1920-04-16|1924-03-18|Coogan Jesse|Apparatus and method of extracting the petroleum content from petroleum-bearing sand or shale|
    US3846276A|1973-06-18|1974-11-05|Texaco Inc|Process for separating bitumen from tar sand recovered from deposits by mining|IT1147716B|1980-02-15|1986-11-26|Rtl Contactor Holding Sa|PROCESSING PROCESS FOR HETEROGENEOUS LIQUID MATERIALS PARTICULARLY FOR THE PURPOSE OF EXTRACTION OF OLIBITUMINOSES FROM SANDS CONTAINING THEM|
    WO1984002145A1|1982-11-22|1984-06-07|Solv Ex Corp|A process and apparatus for extracting bitumen oil from bitumen containing mineral|
    US5143598A|1983-10-31|1992-09-01|Amoco Corporation|Methods of tar sand bitumen recovery|
    CA1249976A|1985-06-28|1989-02-14|Bryan D. Sparks|Solvent extraction spherical agglomeration of oilsands|
    BR8504611A|1985-09-20|1987-04-28|Petroleo Brasileiro Sa|PROCESS TO SEPARATE WATER AND SOLIDS FROM FUELS, IN PARTICULAR FROM SHALE OIL|
    US4692238A|1986-08-12|1987-09-08|Institute Of Gas Tehnology|Solvent extraction of organic oils and solvent recovery|
    CA2123076C|1994-05-06|1998-11-17|William Lester Strand|Oil sand extraction process|
    US5723042A|1994-05-06|1998-03-03|Bitmin Resources Inc.|Oil sand extraction process|
    US6712215B2|2000-07-28|2004-03-30|Adolf Frederik Scheybeler|Method and apparatus for recovery of lost diluent in oil sands extraction tailings|
    US7381320B2|2004-08-30|2008-06-03|Kellogg Brown & Root Llc|Heavy oil and bitumen upgrading|
    US7749378B2|2005-06-21|2010-07-06|Kellogg Brown & Root Llc|Bitumen production-upgrade with common or different solvents|
    CA2512106C|2005-07-13|2008-08-19|Bitmin Resources Inc.|Oil sand processing apparatus and control system|
    US7984866B2|2005-09-23|2011-07-26|Canadian Oil Sands Limited Partnership|Relocatable oil sand slurry preparation system|
    CA2524110C|2005-10-21|2009-04-14|William L. Strand|Bitumen recovery process for oil sand|
    US20080110805A1|2006-11-10|2008-05-15|Veltri Fred J|Continuous flow separation and aqueous solution treatment for recovery of crude oil from tar sands|
    US20080111096A1|2006-11-10|2008-05-15|Veltri Fred J|Composition for extracting crude oil from tar sands|
    US20080110804A1|2006-11-10|2008-05-15|Veltri Fred J|Slurry transfer line|
    US7694829B2|2006-11-10|2010-04-13|Veltri Fred J|Settling vessel for extracting crude oil from tar sands|
    US7919645B2|2007-06-27|2011-04-05|H R D Corporation|High shear system and process for the production of acetic anhydride|
    US9321967B2|2009-08-17|2016-04-26|Brack Capital Energy Technologies Limited|Oil sands extraction|
    CA2734439A1|2011-03-21|2012-09-21|Shell Internationale Research Maatschappij B.V.|A method for extracting bitumen from an oil sand feed stream|
    US9884997B2|2011-09-30|2018-02-06|Mcw Energy Group Limited|Oil from oil sands extraction process|
    US9296954B2|2013-05-22|2016-03-29|Syncrude Canada Ltd. In Trust For The Owners Of The Syncrude Project As Such Owners Exist Now And In The Future|Treatment of poor processing bitumen froth using supercritical fluid extraction|
    US9447330B2|2013-12-19|2016-09-20|Epic Oil Extractors, Llc|Process for producing crude oil and bitumen products|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB3298976A|GB1527269A|1976-08-07|1976-08-07|Solvent extraction process|
    GB293977|1977-01-25|
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