EP0187947A1 - Procédé pour le raffinage par solvant d'huiles résiduelles - Google Patents

Procédé pour le raffinage par solvant d'huiles résiduelles Download PDF

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Publication number
EP0187947A1
EP0187947A1 EP19850115591 EP85115591A EP0187947A1 EP 0187947 A1 EP0187947 A1 EP 0187947A1 EP 19850115591 EP19850115591 EP 19850115591 EP 85115591 A EP85115591 A EP 85115591A EP 0187947 A1 EP0187947 A1 EP 0187947A1
Authority
EP
European Patent Office
Prior art keywords
solvent
refining
zone
mixture
line
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.)
Granted
Application number
EP19850115591
Other languages
German (de)
English (en)
Other versions
EP0187947B1 (fr
Inventor
Gary Lee Hamilton
Andrei Rhoe
Donald P. Satchell
Joseph Anthony Pisani
George Dan Suciu
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.)
CB&I Technology Inc
Original Assignee
Lummus Crest Inc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from US06/680,924 external-priority patent/US4592831A/en
Application filed by Lummus Crest Inc filed Critical Lummus Crest Inc
Publication of EP0187947A1 publication Critical patent/EP0187947A1/fr
Application granted granted Critical
Publication of EP0187947B1 publication Critical patent/EP0187947B1/fr
Expired legal-status Critical Current

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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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C3/00—Working-up pitch, asphalt, bitumen
    • C10C3/08—Working-up pitch, asphalt, bitumen by selective extraction
    • 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
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/16—Oxygen-containing compounds

Definitions

  • a crude unit is modified for use as a unit for the solvent refining of residue. More particularly, the crude distillation tower of a crude unit is divided into at leas first and second separation zones, with the first zone being converted to receive a mixture of solvent refined oil and refining solvent, and the second zone being converted to receive a mixture of refining solvent and pitch, with refining solven being separated in each of the zones.
  • idle crude distillation units may be converted to units for upgrading of various residue feedstocks by a solvent refining process wherein any pre-existing equipment used in the solvent refining is not operated at a pressure greater than its design pressure.
  • the external condensing can be accomplished by heat exchange against process, air, and/or water. As hereinabove indicated, it is also possible to employ some internal condensing by use of external pump around (circulating solvent reflux) and heat exchange against process, air, and/or water.
  • Unflashed material is withdrawn from drum 21 through line 22 and heated in heat exchanger train C, schematically generally indicated as 23, and then further heated in heater 24, which was previously the crude heater of the pre-existing crude unit.
  • a mixture of pitch and deasphalting solvent is withdrawn from separator 17 through line 41, and is heated in heat exchanger train D, schematically generally indicated as 42, and in heater 24 prior to being introduced through line 43 into the lower section 31 of the combination tower 29.
  • heat exchanger train D schematically generally indicated as 42
  • heater 24 prior to being introduced through line 43 into the lower section 31 of the combination tower 29.
  • the material from heat exchanger trains C & D, respectively, are heated in separate coils in heater 24.
  • Deasphalted oil, still containing some solvent is withdrawn from section 28 of combination tower 29 through line 55 for introduction into a sidestream stripper, schematically generally indicated as 56, which can be one or more of the sidestream strippers which was previously employed for the crude distillation tower.
  • the sidestream stripper 56 is provided with stripping gas, such as nitrogen, through line 57.
  • Deasphalted oil essentially free of deasphalting solvent, is withdrawn from sidestream stripper 56 through line 59 with the deasphalted oil being cooled in heat exchanger train C, prior to being passed to a suitable storage zone and/or further use.
  • Uncondensed gas withdrawn from separater 73 through line 74 is compressed in compressor 75 and recycled as stripping gas for use in the sidestream stripper 56 and the combination tower 29.
  • a portion of the compressed gas from compressor 75, in line 77, is recycled to the air cooler 72 through line 77 for pressure control.
  • the air cooler 72, compressor 75 and separater 73 may be the equipment which previously formed a portion of the crude overhead condensing and gas compression system.
  • deasphalting of the residue in deasphalting separation zone 17 the use of a flash drum 21 1 , and a heater 24 1 are similar to the use of such equipment in the embodiment of Fig. 2 of the drawings.
  • the solvent component employed in line 11 1 is naphtha instead of toluene.
  • the mixture of deasphalted oil and deasphalting solvent in line 27 1 is introduced into a combination tower 101, which was previously the crude distillation tower of a crude unit.
  • the tower is modified so as to provide a second zone comprised of sections 102 and 110 for separating deasphalting solvent from pitch, and a first zone comprised of sections 103, 104 and 105 for separating deasphalting solvent from the deasphalted oil, as well as for separating the naphtha portion of the deasphalting solvent from the methanol portion.
  • Fig. 4 of the drawings Still another embodiment of the present invention is shown in Fig. 4 of the drawings.
  • the deasphalting solvent is comprised of components which have similar boiling points which need not be independently added to the oil.
  • the embodiment of Fig. 4 incorporates further improvements in a solvent refining process.
  • the pitch comprised of resins and asphaltenes in combination with deasphalting solvent is withdrawn from section 206 through line 213, and the lighter portion, comprised of resin and some deasphalted oil in deasphalting solvent is withdrawn from section 206 through line 207 for recycle to section 205.
  • the lower section 226 is provided with a stripping gas, such as nitrogen through line 234, and with a solvent wash through line 235.
  • the section 226 is designed and operated so as to separate the deasphalting solvent from the pitch.
  • the ; pitch is withdrawn from section 226 through line 236 and is cooled in heat exchanger train B prior to being passed to a suitable accumulation zone (not shown) for disposal or suitable! use.
  • Deasphalting solvent which has been separated from the pitch in section 226 of combination tower 223 is withdrawn through line 238 .
  • the deasphalted oil is withdrawn from sidestream stripper 248 through line 251 and is cooled in heat exchange train C, prior to being passed to storage and/or further use.
  • Condensed solvent recovered through line 261 is introduced into the tank 254.
  • Solvent vapor which is recovered from pitch and deasphalted oil is condensed at a low pressure (less than 100 PSIG) for reuse in the process.
  • Solvent is withdrawn from storage tank 254 through line 265, with a portion thereof being employed in line 266 for use as solvent wash in the combination tower 223, and the remaining portion being employed in lines 202 and 212 as hereinabove described.
  • FIG. 5 A further embodiment of the present invention is shown in Figure 5 of the drawings.
  • the deasphalting solvent is comprised of components which have similar boiling points which need not be independently added to the oil.
  • the solvent is recovered by use of a multiple effect flash evaporation system.
  • a pitch comprised of resins and asphaltenes in combination with deasphalting solvent is withdrawn from separator 404 through line 405, and the lighter portion, comprised of deasphalted oil in deasphalting solvent is withdrawn from separator 404 through line 406.
  • the multiple effect evaporator is comprised of a low pressure section 413, and medium pressure section 412, both located in the combination tower 411, as well as a high pressure section, located in an extraneous vessel, as hereinafter described.
  • Deasphalted oil still containing some deasphalting solvent, is withdrawn from the medium pressure section 412 through line 421 and heated in heat exchanger 422 and fired heater 423 (which may be the crude heater of the prior crude unit), prior to being introduced into high pressure-vessel 424, which is the third stage of the multiple effect evaporation system for recovering deasphalting solvent from deasphalted oil.
  • the high pressure flash vessel 424 is operated at a pressure of from 65 to 85 psig.
  • Deasphalting solvent is withdrawn from high pressure flash vessel 424 through line 425.
  • Deasphalting solvent which has been separated from pitch in section 414 is withdrawn therefrom through line 447.
  • Deasphalting solvent in line 447 is combined with deasphalting solvent in line 443, and the combined stream is suitably cooled (not shown) so as to condense the solvent for introduction into a solvent vessel 451 through line 452.
  • Flashed deasphalting solvent from the high pressure flash section 424 heats feed to the medium pressure flash section 412 in exchanger 417, and flashed solvent from the medium pressure section 412 heats feed to the low pressure flash section 413 in exchanger 407, and the flashed solvent from sections 412 and 424 may be further cooled (not shown) to effect condensation thereof.
  • Flashed solvent from low pressure section 413 in line 415 is also cooled (not shown) to condense the flashed solvent.
  • the condensed flashed solvent from sections 412, 413 and 424 are combined in line 453 for introduction into the solvent storage vessel 45 1 .
  • Deasphalting solvent is withdrawn from storage vessel 451 through line 402 for use in deasphalting, as hereinabove described.
  • Any uncondensed solvent, as well as nitrogen gas is withdrawn from vessel 451 through line 454 for further treatment to recover nitrogen and provide additional condensed solvent in a manner similar to that described with respect to previous embodiments.
  • the present invention has been particularly described with reference to use of equipment in a pre-existing crude distillation unit, the scope of the invention is not limited thereby.
  • the process may be accomplished with new equipment or by using only a portion of the pre-existing equipment.
  • there may be other low pressure equipment and in particular fractionators which can be converted for use In solvent refining of residues. Accordingly, although it is preferred to use idle equipment in a pre-existing crude distillation unit, the scope of the invention is not limited thereby.
  • the solvent refining unit may be employed to clean an atmospheric residue feed to a residue cat cracker.
  • a residue cat cracker In such an operation, fairly high yields of refined oil can be recovered. As a result, the asphalt yield will be low and may be primarily used as a solid pitch fuel.
  • a vacuum residue may be treated by the solvent refining process, as hereinabove described, with deasphalted oil being employed as a feed to a hydrocracker. This would be similar to the scheme in which a vacuum residue is treated as a feed for a fluid cat cracker, as hereinabove described.
  • a vacuum residue may be treated by the solvent refining process, and deasphalted oil is employed as a feed to a visbraking operation. This would be similar to the: operation in which deasphalted oil is employed as a feed to a cat cracker, as hereinabove described.
  • deasphalted oil from the solvent refining process as hereinabove described may be initially subjected to hydrodesulfurization or to hydrotreating so as to reduce the amount of metals, residual carbon, nitrogen and sulfur compounds contained in the oil, whereby a higher yield of deasphalted oil may be produced as feed to a fluid cat cracker or hydrocracker.
  • the asphalt or pitch quantity recovered from the solvent refining unit will be lower, and will be most suitable for use as a solid pitch fuel.
  • the pitch recovered from the solvent recovery unit can be subjected to delayed coking, thus reducing the amount of solid fuel, and producing gas oil which can be employed as fuel.
  • the present invention is particularly advantageous in that solvent refining of residues can be accomplished in equipment which exists in idle units, such as crude distillation units, without exceeding the design pressure for such units. Such a result can be economically achieved while effectively removing impurities.

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  • 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)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP19850115591 1984-12-12 1985-12-07 Procédé pour le raffinage par solvant d'huiles résiduelles Expired EP0187947B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US68089784A 1984-12-12 1984-12-12
US06/680,924 US4592831A (en) 1984-12-12 1984-12-12 Solvent for refining of residues
US680924 1984-12-12
US680897 1984-12-12

Publications (2)

Publication Number Publication Date
EP0187947A1 true EP0187947A1 (fr) 1986-07-23
EP0187947B1 EP0187947B1 (fr) 1989-02-08

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP19850115591 Expired EP0187947B1 (fr) 1984-12-12 1985-12-07 Procédé pour le raffinage par solvant d'huiles résiduelles

Country Status (3)

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EP (1) EP0187947B1 (fr)
CA (1) CA1263625A (fr)
DE (1) DE3568185D1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013019418A3 (fr) * 2011-07-29 2013-10-10 Saudi Arabian Oil Company Procédé de stabilisation d'hydrocarbures lourds
WO2023100139A1 (fr) * 2021-12-03 2023-06-08 Sabic Global Technologies B.V. Procédés d'élimination de contaminants de silicium et de chlorure à partir d'huile de pyrolyse à base de déchets plastiques mixtes

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3414506A (en) * 1963-08-12 1968-12-03 Shell Oil Co Lubricating oil by hydrotreating pentane-alcohol-deasphalted short residue
GB1173044A (en) * 1966-04-05 1969-12-03 Universal Oil Prod Co Improved Solvent Extraction Process
GB1528837A (en) * 1975-05-15 1978-10-18 Parsons Co Ralph M Solvent deasphalting
GB2134537A (en) * 1983-02-03 1984-08-15 Dravo Corp For solvent deasphalting of petroleum

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3414506A (en) * 1963-08-12 1968-12-03 Shell Oil Co Lubricating oil by hydrotreating pentane-alcohol-deasphalted short residue
GB1173044A (en) * 1966-04-05 1969-12-03 Universal Oil Prod Co Improved Solvent Extraction Process
GB1528837A (en) * 1975-05-15 1978-10-18 Parsons Co Ralph M Solvent deasphalting
GB2134537A (en) * 1983-02-03 1984-08-15 Dravo Corp For solvent deasphalting of petroleum

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013019418A3 (fr) * 2011-07-29 2013-10-10 Saudi Arabian Oil Company Procédé de stabilisation d'hydrocarbures lourds
KR20140064802A (ko) * 2011-07-29 2014-05-28 사우디 아라비안 오일 컴퍼니 중질 탄화수소의 안정화 방법
CN103827267A (zh) * 2011-07-29 2014-05-28 沙特阿拉伯石油公司 用于稳定重质烃的方法
US9493710B2 (en) 2011-07-29 2016-11-15 Saudi Arabian Oil Company Process for stabilization of heavy hydrocarbons
CN108165297A (zh) * 2011-07-29 2018-06-15 沙特阿拉伯石油公司 用于稳定重质烃的方法
KR101886858B1 (ko) * 2011-07-29 2018-08-09 사우디 아라비안 오일 컴퍼니 중질 탄화수소의 안정화 방법
WO2023100139A1 (fr) * 2021-12-03 2023-06-08 Sabic Global Technologies B.V. Procédés d'élimination de contaminants de silicium et de chlorure à partir d'huile de pyrolyse à base de déchets plastiques mixtes

Also Published As

Publication number Publication date
CA1263625A (fr) 1989-12-05
DE3568185D1 (en) 1989-03-16
EP0187947B1 (fr) 1989-02-08

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