US2776931A - Process and apparatus for quenching coker products - Google Patents

Process and apparatus for quenching coker products Download PDF

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Publication number
US2776931A
US2776931A US369455A US36945553A US2776931A US 2776931 A US2776931 A US 2776931A US 369455 A US369455 A US 369455A US 36945553 A US36945553 A US 36945553A US 2776931 A US2776931 A US 2776931A
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Prior art keywords
vapors
temperature
quenching
liquid
solids
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Expired - Lifetime
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US369455A
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English (en)
Inventor
Allen L Chaney
Jr John F Moser
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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Priority to BE530232D priority Critical patent/BE530232A/xx
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Priority to US369455A priority patent/US2776931A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/20—Apparatus in which the axial direction of the vortex is reversed with heating or cooling, e.g. quenching, means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • 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
    • C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal

Definitions

  • the present invention relates to an improved process and apparatus for quenching coker products, i. e., the freshly converted hydrocarbon products obtained by thermally cracking heavy residual hydrocarbon oils.
  • particulate solids which can be fluidized to form a mobile bed. These are preferably of a size between about 40 and about 400 microns, average particle diameter.
  • transfer line coking where preheated solid particles in a relatively disperse phase are used to supply the heat of reaction. In all such cases it is desirable to terminate or substantially terminate the thermal conversion at more or less an optimum point. To accomplish such control and termination of coking reactions without wasteful heat losses is one of the objects of the invention.
  • Another object of the present invention is to utilize heat absorbed in quenching coker products for supplying heat requirements elsewhere in the process. A more particular object is to use such heat to preheat or at least to assist in preheating the heavy oil feed to the system.
  • Heavy residual oils usually contain certain metallic compounds and other ingredients which are highly injurious to cracking catalysts. It is important to avoid, as far as possible, carrying these compounds or ingredients over into the gas oil. At the same time, it is desirable to obtain as much gas oil as practicable, by taking a wide cut of the coker conversion products.
  • Such an apparatus as a vacuum pipe still with steam as a distilling agent to fractionate the coker products, it is possible to obtain a reasonably sharp cut-oil point for the gas oil fraction.
  • Such apparatus is commonly used, in fact, for taking a gas oil fraction from virgin crude oil. In such an operation it is quite satisfactory. The virgin materials are usually quite fully saturated and undesirable side reactions do not take place to any serious extent.
  • quenching or scrubbing at a temperature of the desired range, about 750 to 825 E, without substantial formation of deposits may be obtained by providing a very short holding time for both vapor and liquid at such temperature. This is accomplished by rapidly quenching the efiluent vapors from the coking process, having a temperature somewhere around the general range of 1000 5., down to a temperature of 750 to 825 F., using fresh feed, i. e. a liquid hydrocarbon oil, as quenching medium.
  • the fresh residual feed for example, is usually moderately preheated and hence is usually available at a temperature within the range of about 350 to 600 F.
  • the coker vapors including any solid particles entrained therein, are quenched by scrubbing or spraying them with appropriate quantities of such fresh feed.
  • the coker products both vapor and liquid, i. e. those of boiling range below the original residuum feed, and also some higher boiling material, plus hydrocarbon vapors, are then passed immediately to a vapor-liquid separator, without allowing them time to undergo further or secondary reaction such as a deposit-forming reaction or degradation.
  • the vapors leave the separator, which may be a more or less conventional cyclone, at the quenched temperature and they may be further quenched immediately to any desired lower temperature. Water or other hydrocarbon products may be used for this latter quenching.
  • the liquid thus obtained which includes the fresh feed I Patented Jan. 8, 1957 the coking operation, flows downwardly in the separator, e. g. in the dipleg of a cyclone. If allowed to remain even at its somewhat reduced temperature (750 to 825 F. or so)"thismaterial would soon form such heavy deposits of coke and other polymeric or resinous materials that the separator (cyclone or equivalent) and contiguous apparatuselement's would be clogged.
  • a'n additionalquantityof a quenching material such as water or oil, but preferably more of the fresh feed, at its initial or preheat temperature of 350 to 600 F., is fed'into the bottom of the separator to mix with. and further cool the now down fiowingliquid which has been separated. as mentioned above.
  • Thismixture of preheated fee'd plus quenched liquid above the gas oil boiling range is then conveyed into the coker, the feed thereby including well preheated fresh feed plus recycled heavy ends which. also include the objectionable catalyst contaminants: and other degradation products;
  • the hot vapor products are shown coming from the coking operation into a;conduit.11 at coking temperature, e. g., 950 to 1050 F. or higher.
  • At this temperature considering the vapor pressures of thevariouscomponents, substantially all of the coker efiiuent products boiling above about 1015" F., i. e.- above the gas'oil, are condensed.
  • Themixture of quench and'quenched products passes immediately into the liquid vapor separator 15, shown as a conventional cyclone. They enter atasufficie'nt velocity to separate the uncondensed gas ,oil and lighterrhydrocarbon vapors and gases from the liquidand-from any entrained solids which are carried over from the coking operation by entrainment.
  • the vapors pass overhead through a line 17 to suitable recovery apparatus, not shown, but of conventionaltype.
  • the fresh feed fromline 21 may also be sprayed into the separator itself, especially in the lower portion thereof just above the outlet 19 toprevent building up deposits inside the separator. This will depend upon the type of products being'quenched and the temperatures, as well as the scouring effect or adsorbent effect of entrained solids, etc. It will be understood that other types of separators maybe used instead of the cyclone illustrated, if desired; However, a cyclone as shown has been found to be quite satisfactory.
  • the quenched liquid flowing down the line19 preferably pass into a surge tank 21. This is not always necessary, but is desirable. It actsas a small reservoir to keep a continuous stream ofmaterial'flowing to the out let and thus reduce deposition Withinthe conduits. From the surge or seal pct 21, the efliuent is withdrawn'through a line 23 by a suitable pump not shown. From here the now preheated feed, including the coker bottoms and entrained solids, is taken back to the coker.
  • the invention contemplates heating all or substantially all of the coker feed from an initial preheat temperature of lower range, e. g. 350 to 500 F. up to a higher preheat range, e. g. 500 to 700 F., preferably about 600 F.
  • the temperature limits at each stage may be varied from those given above.
  • the point of introduction of the quenching medium, its initial temperature, and the manner of feeding it may be varied. It may be sprayed into conduits 11, 19, or one or more pools may be formed at appropriate places through which the coker vapors, etc. may be passed for scrubbing as well as quenching, etc.
  • a process for quenching and separating hot efiluent vapors containing a small amount of entrained solids from a high temperature residual oil conversion process employing preheated particulate solids which comprises: quenching said vapors to a temperature in the range of 750 to 825 F. by adding a liquid hydrocarbon oil hav ing a temperature in the. range 350 to 600 F. thereby liquefying the high boiling contaminant containing portion of the vapors, then separating in a cyclonic separation zone liquid and solids from the remaining quenched vapors, recovering said remaining quenched vapors, and immediately further cooling the condensed liquid and solids so separated to a temperature in the range of 500 to 700 F.
  • Apparatus of claim 4 comprising in addition thereto means for maintaining a liquid reservoir of the liquid 10 withdrawn from said separator.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
US369455A 1953-07-21 1953-07-21 Process and apparatus for quenching coker products Expired - Lifetime US2776931A (en)

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BE530232D BE530232A (is") 1953-07-21
US369455A US2776931A (en) 1953-07-21 1953-07-21 Process and apparatus for quenching coker products

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2901418A (en) * 1956-12-03 1959-08-25 Exxon Research Engineering Co Improved quench oil for high temperature coking of residua
US2906690A (en) * 1955-05-16 1959-09-29 Exxon Research Engineering Co Conversion of hydrocarbons
US2927890A (en) * 1957-04-10 1960-03-08 Exxon Research Engineering Co Product stream in quenching conversion system
US2937141A (en) * 1957-09-10 1960-05-17 Gulf Research Development Co Separating volatile components from a heavy oil by means of a venturi tube
US2943994A (en) * 1958-02-14 1960-07-05 Exxon Research Engineering Co Chemicals coking quenching system
US3116231A (en) * 1960-08-22 1963-12-31 Continental Oil Co Manufacture of petroleum coke
US3449212A (en) * 1967-01-09 1969-06-10 Lummus Co Cyclonic cracking vapor heat exchanger inlet for solids removal
US4404092A (en) * 1982-02-12 1983-09-13 Mobil Oil Corporation Delayed coking process
US4863586A (en) * 1987-05-07 1989-09-05 Veba Oel Entwicklungs-Gesellschaft Mbh Process for recovery of low-temperature carbonization oil
WO2020168062A1 (en) * 2019-02-15 2020-08-20 Exxonmobil Chemical Patents Inc. Coke and tar removal from a furnace effluent
EP4144441A1 (en) 2021-09-07 2023-03-08 OMV Downstream GmbH Apparatus and process for separating components of a multiphase hydrocarbon stream

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2405395A (en) * 1943-07-31 1946-08-06 Standard Oil Co Acetylene process
US2422501A (en) * 1944-12-08 1947-06-17 Standard Oil Dev Co Apparatus for carrying out chemical reactions in the presence of finely-divided powder
US2471104A (en) * 1944-11-10 1949-05-24 Standard Oil Dev Co Production of unsaturated hydrocarbons and hydrogen
US2487176A (en) * 1945-04-24 1949-11-08 Solar Aircraft Co System for recovering water from exhaust gas
US2608526A (en) * 1946-12-14 1952-08-26 Standard Oil Dev Co Coking of carbonaceous fuels
US2698672A (en) * 1952-10-15 1955-01-04 Standard Oil Dev Co Cyclone separator for separating solid particles from gasiform mixtures

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2405395A (en) * 1943-07-31 1946-08-06 Standard Oil Co Acetylene process
US2471104A (en) * 1944-11-10 1949-05-24 Standard Oil Dev Co Production of unsaturated hydrocarbons and hydrogen
US2422501A (en) * 1944-12-08 1947-06-17 Standard Oil Dev Co Apparatus for carrying out chemical reactions in the presence of finely-divided powder
US2487176A (en) * 1945-04-24 1949-11-08 Solar Aircraft Co System for recovering water from exhaust gas
US2608526A (en) * 1946-12-14 1952-08-26 Standard Oil Dev Co Coking of carbonaceous fuels
US2698672A (en) * 1952-10-15 1955-01-04 Standard Oil Dev Co Cyclone separator for separating solid particles from gasiform mixtures

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2906690A (en) * 1955-05-16 1959-09-29 Exxon Research Engineering Co Conversion of hydrocarbons
US2901418A (en) * 1956-12-03 1959-08-25 Exxon Research Engineering Co Improved quench oil for high temperature coking of residua
US2927890A (en) * 1957-04-10 1960-03-08 Exxon Research Engineering Co Product stream in quenching conversion system
US2937141A (en) * 1957-09-10 1960-05-17 Gulf Research Development Co Separating volatile components from a heavy oil by means of a venturi tube
US2943994A (en) * 1958-02-14 1960-07-05 Exxon Research Engineering Co Chemicals coking quenching system
US3116231A (en) * 1960-08-22 1963-12-31 Continental Oil Co Manufacture of petroleum coke
US3449212A (en) * 1967-01-09 1969-06-10 Lummus Co Cyclonic cracking vapor heat exchanger inlet for solids removal
US4404092A (en) * 1982-02-12 1983-09-13 Mobil Oil Corporation Delayed coking process
US4863586A (en) * 1987-05-07 1989-09-05 Veba Oel Entwicklungs-Gesellschaft Mbh Process for recovery of low-temperature carbonization oil
WO2020168062A1 (en) * 2019-02-15 2020-08-20 Exxonmobil Chemical Patents Inc. Coke and tar removal from a furnace effluent
CN113423803A (zh) * 2019-02-15 2021-09-21 埃克森美孚化学专利公司 从炉流出物去除焦炭和焦油
US11932816B2 (en) 2019-02-15 2024-03-19 Exxonmobil Chemical Patents Inc. Coke and tar removal from a furnace effluent
EP4144441A1 (en) 2021-09-07 2023-03-08 OMV Downstream GmbH Apparatus and process for separating components of a multiphase hydrocarbon stream
WO2023036751A1 (en) 2021-09-07 2023-03-16 OMV Downstream GmbH Apparatus and process for separating components of a multiphase hydrocarbon stream

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