KR890008302A - Heavy oil cracking process and oil fraction produced by this process - Google Patents

Heavy oil cracking process and oil fraction produced by this process Download PDF

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Publication number
KR890008302A
KR890008302A KR1019880015525A KR880015525A KR890008302A KR 890008302 A KR890008302 A KR 890008302A KR 1019880015525 A KR1019880015525 A KR 1019880015525A KR 880015525 A KR880015525 A KR 880015525A KR 890008302 A KR890008302 A KR 890008302A
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South Korea
Prior art keywords
process according
hydrogen
metal
oil fraction
catalyst
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KR1019880015525A
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Korean (ko)
Inventor
티옹 시이 스완
피이터 드 종 크리옌
쥴리앙 쟝 뒤푸르 쟈끄
Original Assignee
오노 알버어스
셀 인터나쵸 나아레 레사아치 마아츠샤피 비이부이
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Publication of KR890008302A publication Critical patent/KR890008302A/en

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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/14—Inorganic carriers the catalyst containing platinum group metals or compounds thereof
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers

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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)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
  • Fats And Perfumes (AREA)

Abstract

내용 없음No content

Description

중유 분해 공정 및 이 공정에 의해 제조된 오일 분류물Heavy oil cracking process and oil fraction produced by this process

본 내용은 요부공개 건이므로 전문내용을 수록하지 않았음Since this is an open matter, no full text was included.

Claims (15)

400-550℃, 바람직하게는 410-530℃, 더 바람직하게는 440-510℃에서 10-60바아(바람직하게는 20-40바아)의 수소 분압하에서 비-산성 수소 활성화 촉매를 함유하는 반응 지대를 통하여 수소를 함유하는 기체 유동과 함께 저함량의 아스팔트 성분을 갖는 중유 분류물을 통과시키는 것을 포함하는 중유 분류물을 경유 분류물로 전환시키는 방법.Reaction zone containing a non-acidic hydrogen activation catalyst at a hydrogen partial pressure of 10-60 bar (preferably 20-40 bar) at 400-550 ° C., preferably 410-530 ° C., more preferably 440-510 ° C. Converting the heavy oil fraction into a diesel fraction comprising passing through a heavy oil fraction having a low asphalt content with a gas flow containing hydrogen therethrough. 제1항에 있어서, 중유 분류물이 3%w 미만, 바람직하게는 2%w 미만, 더욱 바람직하게는 1%w 미만의 아스팔트 성분의 함량을 갖는 방법.The method of claim 1, wherein the heavy oil fraction has a content of asphalt components of less than 3% w, preferably less than 2% w, more preferably less than 1% w. 제1항 또는 제2항에 있어서, 중유 분류물이 실질적으로 350 내지 580℃의 비점을 갖는 (합성) 증류물 또는 합성 탈아스팔트 오일인 방법.The process according to claim 1 or 2, wherein the heavy oil fraction is a (synthetic) distillate or synthetic deasphalted oil having a boiling point of substantially 350 to 580 ° C. 제1항 또는 제2항에 있어서, 중유 분류물이 중잔류물을 열분해시킴으로써 얻어진 350 내지 520℃에서 실질적으로 끓는 증류물인 방법.The process according to claim 1 or 2, wherein the heavy oil fraction is a distillate boiling substantially at 350 to 520 ° C. obtained by pyrolyzing the heavy residue. 제1항 내지 제4항중 어느 한 항에 있어서, 촉매 1개이상의 VIII족 귀금속, 바람직하게는 팔라듐 또는 플래듐을 포함하는 방법.5. The process according to claim 1, comprising at least one catalyst of Group VIII precious metals, preferably palladium or platdium. 6. 제1항 내지 제5항중 어느 한 항에 있어서, 촉매가 바람직하게는 금속 황화물 형태로 1개 이상의 IVa족 금속, 특히 주석, 1개 이상의 VIb족 금속, 특히 몰리브덴, 크롬 또는 텅스텐, 및/또는 1개 이상의 VIII족 금속, 특히 철, 코발트, 또는 니켈을 포함하는 방법.The catalyst according to claim 1, wherein the catalyst is preferably in the form of metal sulfides of at least one Group IVa metal, in particular tin, at least one Group VIb metal, in particular molybdenum, chromium or tungsten, and / or 1 At least one Group VIII metal, in particular iron, cobalt, or nickel. 제6항에 있어서, 촉매가 바람직하게는 금속의 황화물 형태로 철, 코발트 또는 티켈로부터 선택된 한개 이상의 금속과 1개 이상의 IVb족 금속, 특히 몰리브덴, 크롬 또는 텅스텐을 포함하는 방법.The process according to claim 6, wherein the catalyst comprises at least one metal selected from iron, cobalt or titanium and at least one Group IVb metal, in particular molybdenum, chromium or tungsten, in the form of sulfides of the metal. 제5항 내지 제7항중 어느 한 항에 있어서, 촉매가 뚜렷하나 제한된 수소화 탈황활성을 보이는 방법.8. The process according to any one of claims 5 to 7, wherein the catalyst exhibits a pronounced but limited hydrodesulfurization activity. 제5항 내지 제8항중 어느 한 항에 있어서, 촉매가 바람직하게는 적어도 0.2ml/g, 특히 적어도 0.5ml/g의 기공 부피를 갖는, 금속이 부착되는 담체를 포함하는 방법.9. The process according to claim 5, wherein the catalyst comprises a carrier to which a metal is attached, preferably having a pore volume of at least 0.2 ml / g, in particular at least 0.5 ml / g. 제1항 내지 제9항중 어느 한 항에 있어서, 공급물의 공간속도가 0.1 내지 5l/l/h, 바람직하게는 0.5 내지 3l/l/h이며 수소속도가 100-2000Nl/kg, 바람직하게는 100-500Nl/kg, 더욱 바람직하게는 200-400Nl/kg인 방법.10. The space velocity of the feed is 0.1 to 5 l / l / h, preferably 0.5 to 3 l / l / h and the hydrogen rate is 100-2000 Nl / kg, preferably 100. -500Nl / kg, more preferably 200-400Nl / kg. 제1항 내지 제10항중 어느 한 항에 있어서, 수소 함유 유동이 수소량의 50%(v/v)까지, 바람직하게는 1 내지 30%, 더 바람직하게는 5내지 25%의 양인 황화 수소와 수소인 혼합물을 포함하는 방법.The hydrogen sulfide according to any one of claims 1 to 10, wherein the hydrogen-containing flow is up to 50% (v / v) of the amount of hydrogen, preferably 1 to 30%, more preferably 5 to 25%. A mixture comprising hydrogen. 제1항 내지 제11항중 어느 한 항에 있어서, 반응이 고정상 조작으로 바람직하게는 위로 흐르는 양식으로 수행되는 방법.The process according to claim 1, wherein the reaction is carried out in a stationary phase operation, preferably in a flowing stream. 제1항 내지 제12항중 어느 한 항에 있어서, 반응 생성물 내에 존재하는 비전환 물질의 적어도 일부분이 재순환되는 방법.The method of claim 1, wherein at least a portion of the nonconverting material present in the reaction product is recycled. 제1항 내지 제13항중 어느 한 항에 있어서, 반응의 비전환된 물질이 유동화 촉매 분해 반응에 대한 공급물로서 사용되는 방법.The process according to claim 1, wherein the unconverted material of the reaction is used as feed for the fluidized catalytic cracking reaction. 제1항 내지 제14항중 어느 한 항에 있어서 기술된 방법에 따라 제조된 오일 분류물.An oil fraction prepared according to the method of any one of claims 1-14. ※ 참고사항 : 최초출원 내용에 의하여 공개하는 것임.※ Note: The disclosure is based on the initial application.
KR1019880015525A 1987-11-27 1988-11-24 Heavy oil cracking process and oil fraction produced by this process KR890008302A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB878727777A GB8727777D0 (en) 1987-11-27 1987-11-27 Heavy oil cracking process
GB8727777 1987-11-27

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KR890008302A true KR890008302A (en) 1989-07-10

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EP (1) EP0318125B1 (en)
JP (1) JPH01170689A (en)
KR (1) KR890008302A (en)
CN (1) CN1022043C (en)
AR (1) AR244309A1 (en)
AT (1) ATE76893T1 (en)
AU (1) AU608389B2 (en)
BR (1) BR8806191A (en)
CA (1) CA1326464C (en)
DD (1) DD283643A5 (en)
DE (1) DE3871732T2 (en)
DK (1) DK655488A (en)
ES (1) ES2032004T3 (en)
FI (1) FI885467A (en)
GB (1) GB8727777D0 (en)
GR (1) GR3004811T3 (en)
IN (1) IN173572B (en)
MX (1) MX172342B (en)
MY (1) MY104114A (en)
NO (1) NO172898C (en)
NZ (1) NZ227067A (en)
PH (1) PH25825A (en)
RU (1) RU1813095C (en)
SG (1) SG45793G (en)
ZA (1) ZA888798B (en)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1045462C (en) * 1996-07-22 1999-10-06 中国石油化工总公司 Middle-pressure hydrocracking process for heavy fractional oil
CN1045100C (en) * 1996-12-26 1999-09-15 南京兴达石油化工科技工贸公司 Method for producing special kerosene type solvent naphtha
NL1027784C2 (en) * 2003-12-19 2006-08-23 Shell Int Research Systems and methods for preparing a crude product.
US20050133405A1 (en) 2003-12-19 2005-06-23 Wellington Scott L. Systems and methods of producing a crude product
US20090065394A1 (en) * 2007-09-07 2009-03-12 Uop Llc, A Corporation Of The State Of Delaware Hydrocracking process for fabricating distillate from fisher-tropsch waxes
JP5526408B2 (en) 2010-01-19 2014-06-18 国立大学法人東北大学 Fuel property determination method and fuel property determination device
JP5453221B2 (en) 2010-11-18 2014-03-26 国立大学法人東北大学 Combustion experiment equipment

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US2801208A (en) * 1954-02-04 1957-07-30 Gulf Research Development Co Process for hydrogen treatment of hydrocarbons
FR1568754A (en) * 1967-06-30 1969-05-30
DE2504248A1 (en) * 1974-02-07 1975-08-21 Exxon Research Engineering Co CATALYST MIXTURE AND PROCESS FOR THE CONVERSION OF HEAVY PETROLEUM RAW MATERIALS
US4298458A (en) * 1980-02-25 1981-11-03 Mobil Oil Corporation Low pressure hydrotreating of residual fractions

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Publication number Publication date
CN1022043C (en) 1993-09-08
ES2032004T3 (en) 1993-01-01
DK655488D0 (en) 1988-11-24
EP0318125A2 (en) 1989-05-31
GB8727777D0 (en) 1987-12-31
NO885257L (en) 1989-05-29
EP0318125B1 (en) 1992-06-03
NO172898B (en) 1993-06-14
DK655488A (en) 1989-05-28
SG45793G (en) 1993-06-25
JPH01170689A (en) 1989-07-05
CA1326464C (en) 1994-01-25
BR8806191A (en) 1989-08-15
FI885467A (en) 1989-05-28
AR244309A1 (en) 1993-10-29
ATE76893T1 (en) 1992-06-15
IN173572B (en) 1994-06-04
RU1813095C (en) 1993-04-30
MY104114A (en) 1993-12-31
CN1033831A (en) 1989-07-12
AU608389B2 (en) 1991-03-28
NO172898C (en) 1993-09-22
ZA888798B (en) 1989-07-26
DE3871732D1 (en) 1992-07-09
PH25825A (en) 1991-11-05
DE3871732T2 (en) 1993-01-21
MX172342B (en) 1993-12-14
AU2589288A (en) 1989-06-01
DD283643A5 (en) 1990-10-17
NO885257D0 (en) 1988-11-24
EP0318125A3 (en) 1990-03-14
FI885467A0 (en) 1988-11-24
NZ227067A (en) 1990-08-28
GR3004811T3 (en) 1993-04-28

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