EP0193222A2 - Procédé et appareillage pour le craquage thermique d'huiles hydrocarburées et mélange d'hydrocarbures préparé ainsi - Google Patents

Procédé et appareillage pour le craquage thermique d'huiles hydrocarburées et mélange d'hydrocarbures préparé ainsi Download PDF

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Publication number
EP0193222A2
EP0193222A2 EP86200137A EP86200137A EP0193222A2 EP 0193222 A2 EP0193222 A2 EP 0193222A2 EP 86200137 A EP86200137 A EP 86200137A EP 86200137 A EP86200137 A EP 86200137A EP 0193222 A2 EP0193222 A2 EP 0193222A2
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EP
European Patent Office
Prior art keywords
process according
gaseous materials
conversion zone
withdrawn
hydrocarbon oil
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.)
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Application number
EP86200137A
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German (de)
English (en)
Other versions
EP0193222A3 (fr
Inventor
Jean François Robert Arsene Larive
Clas Ingemar Wernersson
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0193222A2 publication Critical patent/EP0193222A2/fr
Publication of EP0193222A3 publication Critical patent/EP0193222A3/fr
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    • 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
    • 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
    • C10G9/06—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by pressure distillation

Definitions

  • the present invention relates to a process for the continuous thermal cracking of hydrocarbon oils and to hydrocarbon mixtures thus prepared.
  • thermal cracking can be suitably applied to convert residual oils into lighter products.
  • furnace cracking implies that the actual cracking takes place at the downstream end of a furnace and to some extent in the transfer line between the furnace and a subsequent treating.unit.
  • the residence time of the feedstock is relatively short, of the order of only one minute.
  • soaker cracking In the case of soaker cracking the feed is heated to a suitable temperature, which is considerably lower than the temperature applied in furnace cracking, and the feed is allowed to stay at that temperature for a period usually between 5 and 60 minutes in a thermal conversion vessel normally referred to as a soaker.
  • a soaker can be defined as a vessel without supplementary heating, which vessel allows cracking to take place over a prolonged period. No heat is provided to the soaker and, since the cracking reaction is endothermic, the temperature of the feed drops by about 10-30 °C during passage through the soaker.
  • Soaker cracking has staged a successful come-back as a convenient and relatively inexpensive step towards reducing fuel oil residues and compares favourably with furnace cracking with respect to capital costs, fuel consumption and onstream times.
  • One of the factors unfavourably governing the product pattern of thermally cracked material is the degree of over-cracking which may occur when valuable products are maintained too long under cracking conditions, for instance during transport through a soaking vessel (necessary to accomplish a reasonable conversion of unconverted material), especially when substantial amounts of such products had already been formed during the heating and transporting stage of the feed, in particular when the feed had been subjected for a considerable period of time to cracking conditions.
  • the object of the present invention is therefore to reduce or even prevent over-cracking and thus optimizing the product yield by removing valuable materials produced or present as quickly as possible.
  • the present invention therefore relates to a process for the continuous thermal cracking of hydrocarbon oils by heating a hydrocarbon oil and causing it to flow through a thermal conversion zone, wherein at least part of the gaseous materials produced during said heating is withdrawn from the heated oil prior to its introduction into a thermal conversion zone.
  • the removal of at least part of the gaseous materials produced prior to introduction of the heated hydrocarbon oil into a thermal cracking zone has a number of advantages. Not only will the product yield pattern improve substantially, it is also possible to operate the thermal conversion zone under optimum conditions with respect to further conversion of unconverted feed since a substantial part of the material normally introduced into the soaking vessel is now directly transported for final processing or directly used in a different (hydro)conversion operation. It is also possible to allow more cracking during the early stage of the thermal cracking process since the products can now be removed prior to the conversion of unconverted feed.
  • phase-separator The withdrawal of gaseous materials according to the process according to the present invention is suitably carried out by a phase-separator.
  • Cyclones are examples of suitable phase-separators which can be used advantageously in the process according to the present invention. They are well-known to those skilled in the art.
  • the capacity of the cyclone to be used will largely depend on the severity of the thermal cracking to be achieved in the early stage of the thermal cracking process.
  • the cyclones to be used should be capable of conveniently separating amounts of gaseous materials produced corresponding with amounts of vapour up to 80 %wt calculated on hydrocarbon oil to be processed.
  • the thermal cracking according to the present invention is suitably performed at a temperature in the range between 350 and 550 °C, preferably at a temperature between 400 and 500 °C.
  • the temperature at which the cyclone will be operated will be substantially the same as the outlet of the upstream heating zone (which may include a soaking vessel) and is some 20-40 °C higher than the temperature of the cracked product leaving the thermal conversion zone.
  • gaseous material produced In order to facilitate further processing, it is preferred to withdraw substantially all of the gaseous material produced prior to introduction of the remaining material into the thermal conversion zone.
  • the gaseous material removed may be subjected to further physical separation treatment(s) depending on the intended use of the products obtained.
  • the heated hydrocarbon oil depleted of gaseous materials according to the process according to the present invention is passed to the thermal conversion zone, preferably a soaking vessel, in-order to continue the thermal conversion of yet unconverted material present therein. It is advantageous to transport the oil to be converted by means of gravity to the soaking vessel since the use of control-equipment will then be reduced or may even not be necessary at all.
  • soaking vessels not containing internals can be used in the process according to the present invention, preference is given to the use of soaking vessels containing internals as described in European patent specification 7656.
  • Good results will be obtained when the bottom product of the phase-separator, i.e. heated hydrocarbon oil depleted of gaseous materials, is caused to flow upwardly through a soaking vessel provided with horizontal perforated plates, which effectively increase the number of mixing stages.
  • the number of plates is preferably in the range of from 1 to 20. To achieve optimal results with the perforated plates, preferably 1-30% of the plate area is occupied by free area.
  • the ratio free area of top plate to the free area of bottom plate is in the range of from 2 to 6.
  • a soaking vessel having its interior divided into a plurality of consecutive, interconnected compartments wherein heated hydrocarbon oil depleted of gaseous materials is caused to pass through the consecutive compartments prior to withdrawal of liquid material from the soaking vessel, and wherein gaseous materials present in the compartments are collected and withdrawn from the vessel.
  • Preferred embodiments of soaking vessels provided with gas withdrawal facilities comprise vertically extending soaking vessels wherein the oil is passed downwardly through the consecutive compartments, in particular through compartments made up of inclined separating walls whilst fluid passages are positioned below the higher parts of the separating walls, which fluid passages are formed by elongated open-ended tubular elements passing through openings in the separating walls as described in said European patent application. It is furthermore beneficial to withdraw the gas present in the soaking vessel via openings in a central discharge system. Also vertically extending soaking vessels wherein the feed is processed in upward flow can be used advantageously.
  • the product.leaving the thermal conversion zone will normally be subjected to phase-separation, e.g. by means of a cyclone.
  • the gaseous products can be subjected to further processing and the bottom product of the phase-separator can be subjected, if desired, to a further thermal conversion in a suitable soaking vessel or can be subjected to further processing.
  • Suitable quench fluids comprise the usual quenching means, such as hydrocarbon oils. Steam may also be used to assist in phase-separation.
  • soaker cracking has the advantage that a selected constant pressure can be applied.
  • This pressure is normally chosen up to 30 bar gauge, preferably up to 15 bar gauge.
  • a residual oil feedstock is passed through a line 1 to a furnace 2 where it is heated to a temperature in the range of from '350-550°C.
  • the hot feed already partially converted, is passed through a line 3 to a phase-separator 4.
  • Gaseous materials are withdrawn from the top of the phase-separator (cyclone) via a line -5 for further processing (not shown).
  • the bottom product discharged from the cyclone is passed, preferably by gravity, through a line 6 to a soaking vessel 7 in which it flows upwards through horizontal perforated plates 8.
  • the cracked product leaves the soaking vessel at the top via a line 9 through which it is transferred to a further processing stage which may include a further phase-separator (not shown) to produce valuable products (gasoline, heating oils and fuel oil).
  • a further processing stage which may include a further phase-separator (not shown) to produce valuable products (gasoline, heating oils and fuel oil).
  • soaking vessels as described in European patent application 84201250 referred to hereinbefore can also be applied.
  • the additional benefit in terms of "fuel reduction” is estimated to be between 0.5 and 1.0 y m on feed.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP86200137A 1985-02-25 1986-01-31 Procédé et appareillage pour le craquage thermique d'huiles hydrocarburées et mélange d'hydrocarbures préparé ainsi Withdrawn EP0193222A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8504807 1985-02-25
GB858504807A GB8504807D0 (en) 1985-02-25 1985-02-25 Thermal cracking of hydrocarbon oils

Publications (2)

Publication Number Publication Date
EP0193222A2 true EP0193222A2 (fr) 1986-09-03
EP0193222A3 EP0193222A3 (fr) 1988-07-20

Family

ID=10575035

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86200137A Withdrawn EP0193222A3 (fr) 1985-02-25 1986-01-31 Procédé et appareillage pour le craquage thermique d'huiles hydrocarburées et mélange d'hydrocarbures préparé ainsi

Country Status (7)

Country Link
EP (1) EP0193222A3 (fr)
JP (1) JPS61195190A (fr)
KR (1) KR860006525A (fr)
CN (1) CN86100830A (fr)
ES (1) ES8705506A1 (fr)
FI (1) FI860791L (fr)
GB (1) GB8504807D0 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991004308A1 (fr) * 1989-09-13 1991-04-04 Antero Ollila Procede pour le craquage thermique d'huile d'hydrocarbure et d'autres reactions liquide/gaz
LT3884B (en) 1994-06-22 1996-04-25 Akcine Bendrove Mazeikiu Nafta Reactor of thermal cracking

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1931757A (en) * 1931-04-20 1933-10-24 Universal Oil Prod Co Process for cracking hydrocarbon oils
FR1386576A (fr) * 1963-07-02 1965-01-22 Gulf Research Development Co Procédé de traitement d'un mélange d'hydrocarbures
US4040943A (en) * 1976-06-30 1977-08-09 Uop Inc. Combination thermal cracking and coking process
US4061562A (en) * 1976-07-12 1977-12-06 Gulf Research & Development Company Thermal cracking of hydrodesulfurized residual petroleum oils
US4316729A (en) * 1977-12-27 1982-02-23 Texaco Inc. Highly efficient cyclone separator
GB8323635D0 (en) * 1983-09-02 1983-10-05 Shell Int Research Continuous thermal cracking of hydrocarbon oils

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991004308A1 (fr) * 1989-09-13 1991-04-04 Antero Ollila Procede pour le craquage thermique d'huile d'hydrocarbure et d'autres reactions liquide/gaz
LT3884B (en) 1994-06-22 1996-04-25 Akcine Bendrove Mazeikiu Nafta Reactor of thermal cracking

Also Published As

Publication number Publication date
GB8504807D0 (en) 1985-03-27
CN86100830A (zh) 1986-08-20
FI860791A7 (fi) 1986-08-26
ES552315A0 (es) 1987-05-01
EP0193222A3 (fr) 1988-07-20
ES8705506A1 (es) 1987-05-01
KR860006525A (ko) 1986-09-11
JPS61195190A (ja) 1986-08-29
FI860791L (fi) 1986-08-26
FI860791A0 (fi) 1986-02-24

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Inventor name: LARIVE, JEAN FRANCOIS ROBERT ARSENE