EP1590423B1 - Verfahren zur hochtemperatur-kurzzeit-destillation von rückstandsöl - Google Patents

Verfahren zur hochtemperatur-kurzzeit-destillation von rückstandsöl Download PDF

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Publication number
EP1590423B1
EP1590423B1 EP03813544A EP03813544A EP1590423B1 EP 1590423 B1 EP1590423 B1 EP 1590423B1 EP 03813544 A EP03813544 A EP 03813544A EP 03813544 A EP03813544 A EP 03813544A EP 1590423 B1 EP1590423 B1 EP 1590423B1
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EP
European Patent Office
Prior art keywords
oil
gas
column
mixer
fraction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP03813544A
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German (de)
English (en)
French (fr)
Other versions
EP1590423A1 (de
Inventor
Hans-Jürgen WEISS
Udo Zentner
Helmut Heurich
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lurgi Lentjes AG
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Lurgi Lentjes AG
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Classifications

    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/043—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by fractional condensation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/06—Gasoil

Definitions

  • the invention relates to a method for high-temperature short-term distillation of a residual oil from the processing of petroleum, natural bitumen or oil sands, wherein the residual oil is mixed with granular, hot coke as a heat transfer medium in a mixer, converted into oil vapor, gas and coke and gases and Vapors from the mixer deducted largely separated from the granular coke, cools gases and vapors and produces a product oil as condensate and gas, and that is withdrawn from the mixer coke heated and recycled as a heat transfer medium in the mixer.
  • a reduction of the pollutants can thus be done in principle by a subsequent vacuum distillation of over 360 ° C boiling product oil, in which a pollutant-containing vacuum residue (VR) and a largely pollutant-free vacuum gas oil (VGO) is obtained.
  • VGO pollutant-containing vacuum residue
  • VGO largely pollutant-free vacuum gas oil
  • the present invention seeks to improve the process for high-temperature short-term distillation of residual oils to the effect that the smallest possible residue fraction can be obtained from the product oil in a technically simple manner in which the unwanted catalyst pollutants are largely concentrated.
  • this object is achieved in that a pollutant-rich residue fraction of the vaporous product oil from the mixer after admixture of water vapor or gas to lower the partial pressure at temperatures below 450 ° C is condensed in a column and withdrawn separately from the residual product oil. Subsequently, the uncondensed product oil vapors from the column can be fed to a fractionation column where the remaining low-emission product oil is decomposed into a VGO and a gasoline / gas oil fraction.
  • the invention makes use of the fact that the entire product oil is present in vapor form at the outlet of the mixing plant and can be separated into the desired fractions by a fractional condensation.
  • the boiling cut between VGO and VR must be set as high as possible between 450 ° C and 650 ° C so that the separated VR fraction contains more than 60% of Conradson Carbon Residue (CCR ) contains more than 70% of the heavy metals nickel (Ni) and vanadium (V) still present in the product oil vapor and more than 80% of the asphaltenes still contained in the product oil vapor.
  • CCR Conradson Carbon Residue
  • the partial pressure of the oil fractions to be separated is reduced by adding water vapor or gas to the column, so that there is a heavy condensate at below 450 ° C. with a boiling point above 450 ° C condenses.
  • the condensation of the low-pollutant VGO (boiling point about 360, boiling point 450 to 650 ° C) and the gasoline / gas oil fraction (boiling range C 5 - to about 360 ° C) can then take place in a second condensation stage at correspondingly lower temperatures.
  • the low-pollutant VGO thus obtained can then be catalytically converted into gasoline and gas oil in a hydrocracker and the heavy condensate can either be returned to the mixing reactor or otherwise used, for example as heavy fuel oil.
  • residue oil having a temperature of from 100 ° C. to 400 ° C. is fed to the mixing reactor (1) through line (4).
  • a conversion temperature of the mixture of 450 ° C to 600 ° C is established.
  • the heat transfer coke in the mixing reactor (1) usually has a particle size in the range of 0.1 to 4 mm, so that a substantial separation of the coke from the gases and oil vapors formed in the mixer takes place at the mixer outlet.
  • the mixer (1) has at least two intermeshing, co-rotating screws.
  • the screws are designed in the manner of a screw conveyor and formed with coiled conveying blades.
  • the hot, largely oil-free, granular coke leaves the mixing reactor (1) at the mixer outlet at a temperature of 450 to 600 ° C and falls through a channel (7) in a Nachentgasungsbunker (8) to which a stripping gas (9) supplied in the lower part can be. Residual gases and vapors can be withdrawn from the Nachentgasungsbunker (8) through the channel (7) upwards. Excess coke is withdrawn via line (2a), wherein a portion of the coke can alternatively be withdrawn via the lines (12a).
  • the coke from line (12) passes via a pneumatic conveying path (10), which is supplied via line (5) combustion air and via line (6) fuel in the collection bunker (2). With the promotion by the pneumatic conveyor line (10) upwards a portion of the coke and / or the delivered fuel is burned at the same time.
  • the coke heated in the pneumatic conveying section (10) passes into the collecting bunker (2), from which exhaust gas is removed through line (11).
  • the coke in the collection bunker (2) has temperatures in the range of 500 to 700 ° C.
  • the gaseous and vaporous products of the mixing reactor (1) are passed through the line (13) in a cyclone (14).
  • a separation of fine coke particles instead, which are passed through line (15) in the Nachentgasungsbunker (8).
  • the gaseous and vaporous products are quenched from the cyclone (14) via line (16) in a column (17) and thereby cooled from 450 to 600 ° C to 350 to 450 ° C.
  • C 4- product gas from the container (23) or steam is introduced. This is the partial pressure of the vapor Lowered product oil so far that condenses there at 350 - 450 ° C, a heavy oil fraction with a boiling point between 450 and 650 ° C, in which almost all pollutants are concentrated. A decomposition or coking of the condensed oil is thus avoided.
  • the column (17) is preferably a quench cooler with multiventuri scrubber connected downstream, in which the gases and vapors originating from the mixing reactor (1) are cooled very efficiently in the co-current method and residual coke dust is washed out with its own condensate.
  • the boiling cut between VGO and VR is set to a temperature as high as possible in the range from 450 to 650 ° C. This is done by the application of gas or water vapor to the top of the column (17) via line (24a) and by the cooling of the gases and vapors by means of cooled heavy oil condensate from line (27a).
  • the heavy oil condensate is withdrawn at a temperature of 350-450 ° C from the bottom of the column (17) through line (27), cooled in a heat exchanger (25) to the required temperature and partly as a cooling / washing medium the top of the column (17) fed again.
  • the remaining part of the heavy oil Kondendates is withdrawn via line (27b) as a product.
  • the heavy oil condensate from line (27b) can then either be returned to the mixing reactor (1) or otherwise used, eg as heavy fuel oil.
  • the uncondensed gas / oil vapor mixture via line (18) is withdrawn. According to a further embodiment of the invention, it can be passed into a fractionation column (19).
  • the remaining product oil is separated into low-emission VGO and a pollutant-free gasoline / gas oil fraction.
  • the VGO with a boiling end of 450-650 ° C is withdrawn via line (21) from the bottom of the fractionation column (19).
  • the VGO thus obtained can then be catalytically converted to gasoline and gas oil in a hydrocracker, not shown.
  • the remaining gas / oil vapor mixture via line (20) in the condenser (22) is cooled and in the container (23) in a gasoline / gas oil fraction having a boiling range of, for example C 5 - 360 ° C and a C 4- gas separated.
  • the gasoline / gas oil fraction is withdrawn via line (26) and partially recycled via line (26b) to the top of the fractionating column (19).
  • the remaining gasoline / gas oil mixture is discharged via line (26a) as a product.
  • the non-condensed C 4 gas is removed from the container (23) via line (24) upwards and partly through line (24 a) in the column (17) returned partly withdrawn as a product via line (24 b).
  • 75 t / h of gas / oil vapor mixture at 550 ° C are passed through line (13) in a cyclone (14) for dedusting.
  • the remaining 25 t / h coke are passed through line (7) together with the heat transfer coke in the Nachentgasungsbunker (8).
  • the gas / oil vapor mixture is passed from the cyclone (14) via line (16) in a column (17), where it is diluted with gas and cooled from 550 ° C to 425 ° C.
  • 65 t / h heavy oil condensate are withdrawn with a boiling point of 600 ° C via line (27) and cooled in a heat exchanger (25) from 425 ° C to 380 ° C.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
EP03813544A 2002-12-19 2003-07-09 Verfahren zur hochtemperatur-kurzzeit-destillation von rückstandsöl Expired - Lifetime EP1590423B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10259450 2002-12-19
DE10259450A DE10259450B4 (de) 2002-12-19 2002-12-19 Verfahren zur Hochtemperatur-Kurzzeit-Destillation von Rückstandsöl
PCT/EP2003/007377 WO2004056942A1 (de) 2002-12-19 2003-07-09 Verfahren zur hochtemperatur-kurzzeit-destillation von rückstandsöl

Publications (2)

Publication Number Publication Date
EP1590423A1 EP1590423A1 (de) 2005-11-02
EP1590423B1 true EP1590423B1 (de) 2007-02-21

Family

ID=32519110

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03813544A Expired - Lifetime EP1590423B1 (de) 2002-12-19 2003-07-09 Verfahren zur hochtemperatur-kurzzeit-destillation von rückstandsöl

Country Status (10)

Country Link
US (1) US7507330B2 (enExample)
EP (1) EP1590423B1 (enExample)
JP (1) JP4365788B2 (enExample)
AT (1) ATE354625T1 (enExample)
AU (1) AU2003250003B2 (enExample)
CA (1) CA2511156C (enExample)
DE (2) DE10259450B4 (enExample)
ES (1) ES2282737T3 (enExample)
MX (1) MXPA05006696A (enExample)
WO (1) WO2004056942A1 (enExample)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2624746C (en) 2007-03-12 2015-02-24 Robert Graham Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
CN107298988B (zh) * 2016-04-14 2019-03-19 中国石油化工股份有限公司 一种炼化吸收稳定工艺及系统
CN107298987B (zh) * 2016-04-14 2019-03-19 中国石油化工股份有限公司 吸收稳定工艺及系统
CN107298986B (zh) * 2016-04-14 2019-05-21 中国石油化工股份有限公司 一种吸收稳定工艺方法
CN107298989B (zh) * 2016-04-14 2019-03-19 中国石油化工股份有限公司 一种吸收稳定工艺及系统
CN107400538B (zh) * 2016-05-21 2019-03-19 中国石油化工股份有限公司 一种焦化吸收稳定工艺和系统
CN107400537B (zh) * 2016-05-21 2019-03-19 中国石油化工股份有限公司 一种焦化吸收稳定工艺和装置
CN107400536B (zh) * 2016-05-21 2019-03-19 中国石油化工股份有限公司 焦化吸收稳定工艺和系统

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4983278A (en) * 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
CA2314586C (en) 1996-09-27 2006-11-14 William Taciuk Thermal apparatus and process for removing contaminants from oil
DE19724074C2 (de) 1997-06-07 2000-01-13 Metallgesellschaft Ag Verfahren zur Hochtemperatur-Kurzzeit-Destillation von Rückstandsölen
DE19959587B4 (de) 1999-12-10 2006-08-24 Lurgi Lentjes Ag Verfahren zur schonenden Kurzzeit-Destillation von Rückstandsölen

Also Published As

Publication number Publication date
MXPA05006696A (es) 2006-03-30
DE50306611D1 (de) 2007-04-05
CA2511156C (en) 2012-04-03
DE10259450B4 (de) 2006-08-10
CA2511156A1 (en) 2004-07-08
WO2004056942A1 (de) 2004-07-08
ES2282737T3 (es) 2007-10-16
AU2003250003A1 (en) 2004-07-14
JP4365788B2 (ja) 2009-11-18
JP2006510757A (ja) 2006-03-30
DE10259450A1 (de) 2004-07-15
US7507330B2 (en) 2009-03-24
EP1590423A1 (de) 2005-11-02
US20060138030A1 (en) 2006-06-29
ATE354625T1 (de) 2007-03-15
AU2003250003B2 (en) 2006-12-21

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