US3291573A - Apparatus for cracking hydrocarbons - Google Patents

Apparatus for cracking hydrocarbons Download PDF

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Publication number
US3291573A
US3291573A US348988A US34898864A US3291573A US 3291573 A US3291573 A US 3291573A US 348988 A US348988 A US 348988A US 34898864 A US34898864 A US 34898864A US 3291573 A US3291573 A US 3291573A
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cracking
steam
hydrocarbon
furnace
passing
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US348988A
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English (en)
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Leonard O Frescoln
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Hercules LLC
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Hercules LLC
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Priority to US348988A priority Critical patent/US3291573A/en
Priority to GB31704/64A priority patent/GB1024005A/en
Priority to NL6409295A priority patent/NL6409295A/xx
Priority to ES0304056A priority patent/ES304056A1/es
Priority to BE653468A priority patent/BE653468A/xx
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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
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C10G9/18—Apparatus
    • C10G9/20—Tube furnaces
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00—Chemistry of hydrocarbon compounds
    • Y10S585/919—Apparatus considerations
    • Y10S585/921—Apparatus considerations using recited apparatus structure
    • Y10S585/924—Reactor shape or disposition

Definitions

  • This invention relates to the pyrolysis of hydrocarbons and more particularly to apparatus and method for the thermal cracking of normally liquid, as well as normally gaseous, hydrocarbons in tubular furnaces.
  • Patent No. 2,914,386 discloses a tubular reaction furnace fired at a plurality of spaced points to give flexible and high tempera-ture control of the reacting fluids and extended tube life
  • Patent No. 2,525,276 discloses a process for the cracking of hydrocarbon oils with a minimum of carbon deposition for the substantial production of olefins and including injection means for normally gaseous as well as normally liquid hydrocarbon feedstock
  • Patent No. 2,904,502 which discloses a process of converting hydrocarbons to obtain high capacity throughput in a tubular furnace with a high yield of liquid products.
  • a principal object of this invention is to provide fundamental improvements in the art which pertain to the factors being sought as heretofore set forth.
  • the accomplishment of this object and others will appear hereinafter, the novel features and combinations being set forth in the appended claims.
  • the present invention provides apparatus for the thermal cracking of normally liquid, as well as normally gaseous, hydrocarbons in a tubular furnace in which the improvement comprises: a tubular cracking furnace having at least one vertical elongated cracking tube disposed therein substantially extending from the bottom to the top of said furnace; a core disposed within the cracking tube.
  • a flute conduit in communication with the furnace having a plurality of communicating heat exchangers disposed therein adapted to be heated by the passage therethrough of flue gas from said furnace; means associated with the heat exchangers for passing hydrocarbon and steam therein and'therethrough to effect a vaporized and superheated mixture; and means associated with the heat exchangers for passing the vaporized and superheated mixture therefrom and into the cracking annulus of the furnace.
  • invention further provides an improved method for operation of the apparatus, which comprises passing a vaporized and superheated hydrocarbon-steam mixture through a vertical, elongated annular cracking zone substantially extending from the bottom to the top of a multiple fired tubular furnace; 'andthe hydrocarbon-steam mixture having been vaporized by heat transfer with flue gas emanating from the furnace and said vaporized mixture having been super-heated to a temperature from about 800 to about 1200 F. by heat transfer with said flue gas.
  • FIG. 1 is a diagrammatic flow chart depicting process and apparatus for cracking a light hydrocarbon feedstock such as naphtha;
  • FIG. 2 is a diagrammatic flow chart depicting process and apparatus for cracking a heavy hydrocarbon feedstock such as crude oil, which may contain undesirable, high boiling point components.
  • Boiler blowdownl 300 lb. water/hr.
  • Furnace 10 tubes-Reaction tube Incoloy alloy 800, 8 in. I.D., wall thickness 0.25 in., and 45 feet long inside the radiant section of the firebox.
  • the naphtha is passed through a line 1 into a pump 2 from which it is passed by a valved line 3 into a naphtha preheater 4.
  • the preheater 4 is a first heat exchanger disposed in an elongated flue conduit 5 with flue gas passing therethrough at an ingress temperature of about 570 F. and an egress temperature of about 450 F.
  • the flue gas emanating from the egress side of the preheater 4 is passed through an induced draft fan to a plant chimney (not shown) through an exit conduit 6.
  • the preheated naphtha leaves preheater 4 at a temperature of about 320 F. through line 7 and is passed into a naphtha vaporizer 8.
  • the primary steam is passed through a line 9 into a valved line 10 into the naphtha vaporizer 8.
  • the vaporizer 8 is a second heat exchanger disposed in the elongated flue conduit 5 with flue ga passing therethrough at an ingress temperature of about 720 F. with the egress end thereof in direct communication With preheater 4 and thusly, possessing approximately its ingress temperature.
  • the naphtha is thoroughly mixed with the steam and vaporized by virtue of passing through the vaporizer 8, and the mixture is passed from the vaporizer through line 11 at a temperature of about 400 F. into a naphtha-steam superheater 12.
  • the superhe-ater 12 is a third heat exchanger disposed in the elongated flue conduit 5 with flue gas passing therethrough at an ingress temperature of about 2200 F. and an egress temperature of about 1680 F.
  • the superheated naphtha-steam mixture is passed from the superheater 12 through line 13 at a temperature of about 1100 F. and pressure of about 70 p.s.i.g into the plurality of reaction tubes represented by 14, which are suspended vertically in the furnace 15, which has a plurality of burners 16 located at various heights up the side Walls of the furnace.
  • the core 17 is concentrically disposed Within each of the reaction tubes 14, which extend throughout the height of the furnace. Similarly, the core extends substantially the length of the reaction tube, thereby defining a final preheat and reaction annulus or cracking zone 18 which extends substantially throughout the height of the furnace.
  • a heater 19 and a boiler 20 Interposed between the naphtha vaporizer 8 and the naphtha-steam superheater 12 is a heater 19 and a boiler 20, the heater and boiler both being disposed in the elongated flue conduit superjaoent and subjacent respectively, to the vaporizer and superheater.
  • the boiler feed water is passed through a line 21 into and through a pump 22 from which it is passed by a valved line 23 into the heater 19.
  • the heater 19 is a fourth heat exchanger with flue gas passing therethrough at an ingress temperature of about 900 F. with the egress end thereof in direct communication with vaporizer 8 and thusly, approximately its ingress temperature.
  • the heated feed water is passed from the heater 19 through line 24 at a temperature of about 380 F. into the boiler 20.
  • the boiler 20 is a fifth heat exchanger with the temperature of the flue gas passing therethrough corresponding to the egress conditions of superheater 12 and ingress conditions of heater 19 since the boiler is interposed between these units in direct communication therewith.
  • Steam and unvaporized water from the boiler 20 are passed through a line 25 at a temperature of about 425 F. into a steam drum 26, thus providing excess process steam for other operation of the plant as desired as well as importantly providing means for substantially reducing the flue gas temperature to an optimum range prior to its entry into the vaporizer 8.
  • Unvaporized water from the steam drum is recirculated back through the boiler 20 through line 26a and pump 26b.
  • Core steam is passed from line 9 through a valved line 27 into the top section of superheater 12 and is passed therefrom through a line 28 at a temperature of about 1300 F into the lower portion of core 17, which is provided with a top opening to permit efliux of the core steam.
  • the furnace 15 is operated under the following approximate range of conditions for the cracking of naphtha:
  • the cracked products emanating from the reaction tubes 14 of the furnace 15 pass through exit conduits 29 and are then passed into a quench tank or suitable heat recovery system (not shown) as desired.
  • the feedstock properties and the products of the cracking operation for the naphtha process are as follows:
  • the naphtha is preheated and flashed at low temperature and in conjunction with part or all of the diluent steam is highly preheated by heat exchange with the hot flue gases flowing from the radiant section of the furnace.
  • the temperature of the steamnaphtha mixture is, at a high heat value, in the range of about 800 to 1200 F. and preferably in the range of about 900 to 1100 F., as it enters the cracking tubes.
  • the final heating and cracking zone extends substantially the entire height of the furnace, all of which contributes to improved thermal efficiency, lower investment cost per given furnace capacity, and operation with a minimum of lost production time for periodic decoking operations, for a wide range of hydrocarbon feedstocks.
  • the procedure for cracking a heavy hydrocarbon feedstock, which contains undesirable high boiling components, such as crude oil, will be described with the furnace, the quantity of hydrocarbon feed to the furnace, the firing and flue arrangements remaining much the same as that described for FIG. 1.
  • the crude oil is passed through a line 30 into and through a pump 31 from which it is passed by a valved line 32 into a crude oil vaporizer 33. Part of the dilution steam is added to the oil at an intermediate point in this vaporizer.
  • the vaporizer 33 is a first heat exchanger disposed in the elongated flue conduit 5 with flue gas passing therethro-ugh.
  • the flue gas emanating from the egress side of the vaporizer 33 is passed through the exit conduit 6 by induced draft to other heat recovery units (not shown) such as a combustion air preheater, or directly to the plant chimney (not shown).
  • the totally or partially vaporized crude oil is passed from the vaporizer 33 at a temperature from about 650 to 750 F. through a line 34 and is passed into a column, or rectification apparatus, 35 at a point above its primary stripping section 36.
  • Steam is passed through a line 37 into a steam preheater 38.
  • the preheater 38 is .a second heat exchanger disposed in the elongated flue conduit 5 with flue gas passing therethrough.
  • a portion of the preheated steam is passed from the preheater 38 at a temperature from about 750 to 1100 F. through a line 39 and is passed into the rectification column 35 at a point above its bottoms preheat section 40.
  • the other portion of the preheated steam is passed from the preheater 38 at the temperature from about 750 to 1100 F. through a valved line 41 and is passed into a high temperature heater 42.
  • the heater 42 is a third heat exchanger disposed in the elongated flue conduit 5 in juxtaposition to the furnace with the very hot flue gas from the furnace passing directly therethrough.
  • the highly heated steam is passed from the heater 42 at a temperature from about 1000 to 1500 F.
  • a valved line 46 passes liquid products from the soaking drum 45 into secondary stripping section 44, the combination of which gives liquid phase cracking with the highly heated overhead gaseous products passing through a line 47 beneath the bottoms preheat section 40.
  • a selective rectification section 48 followed by a condenser 49 operated with liquid reflux are positioned at the top of the rectification column 35.
  • the products from the top of the column 35 are passed through a line 50 into an oil-steam superheater 51.
  • the superheater 51 is a fourth heat exchanger disposed in the elongated flue conduit 5 between the high temperature heater 42 and the steam preheater 38 and similar to the other heaters, has the flue gas passing therethrough.
  • the superheated and vaporized oil-steam mixture is passed from the superheater 51 at a temperature of about 800 to 1100 F. through a line 52 into the plurality of reaction tubes represented by 14.
  • that part of the dilution steam which is added to the oil at an intermediate point in vaporizer 33 is fed thereto through a valved line 53.
  • the heavy bottoms are ultimately removed from the rectification column 35 through a line 54 to residuum recovery (not shown).
  • Hydrogen/ carbon ratio atom/atom 1.75. Comradson carbon, wt. percent 0.94. Bromine No. 2.26. Ash, Wt. percent 0.006.
  • the higher boiling components leaving the bottoms sections of the rectification column contain both aromatic components with essentially no hydrocarbon side chains, aromatics with short and relatively long side chains and/or naphthenic rings, naphthenes, straight and branched chain al'kanes, alkenes, diolefins, etc.
  • the aromatic rings cannot be cracked to produce any substantial amount of ole-fins.
  • the non-aromatic side chains, the naphthenes, alkanes, alkenes, diolefins, etc. can be cracked to produce substantial yields of the desired olefins.
  • a yield loss is incurred in these refiractory bottoms unless some means is employed for recovering the desirable components.
  • the liquid bottoms are subjected to an elevated temperature cracking/stripping operation.
  • alkanes, alkenes, diolefins, and even na-phthenes crack much more readily than do the arc matic ring nuclei. Consequently, as the former [types of units crack into lower molecular weight fragments, their boiling points drop, and they are readily stripped out of the remaining bottoms to be carried into the vapor which eventually enters the cracking tube, by a relatively small amount of superheated stripping steam.
  • the partial flash vaporization, rectification, liquid phase cracking, etc. can be performed in an in-line manner with the cracking furnace, or .as separate off-line operations.
  • the latter may include external means for the heating and additional cracking of the heavy bottoms from the stripping section, external means for stripping the lower molecular Weight cracked products dirom the heavy cracked bottoms by vacuum, or steam stripping, or a combination of both, and means for returning the cracked products to the rectification apparatus below the rectification section but above (the stripping section.
  • the preferred embodiment is the in-line scheme utilizing flue gas heat exchange since this leads to optimum economies and better process control.
  • the cores may be made of heat resistant stainless steel alloys such as stabilized or unstabilized type 310 stainless steel, of other heat resistant alloys such as Incoloy 800 or Inconel, of ceramic materials, or,- when advantageous to do so, of materials which act as catalysts for the cracking reaction.
  • the cores usually have centering spacer lugs on the outside of them, and they can be either plain cylindrical tubes on the outside, or have deflector vanes or scroll work on the outside to improve convective heat transfer rates.
  • the core sizes and designs must in all respects be compatible with the interior size of the cracking tube and the process requirements. In general, the cores are designed so :high heat transfer rates and low carbon formation rates are obtained.
  • annular section between the tube and core to provide the optimum residence time for the cracking reaction to proceed, and to prevent the pressure drop in the reaction zone from exceeding tolerable limits.
  • Annulus widths employed have ranged from 0.25 to 1.5 inches.
  • the feedstock may range from normally gaseous hydrocarbons such as ethane, propane, butane, etc. to relatively high boiling liquid such as crude oil.
  • the portion of the hydrocarbon feedstock which is to be' fed to the cored cracking tubes is substantially totally vaporized before being fed to the cracking tubes, being usually vaporized in contact with part 011' all of the cracking dilution steam. It is then introduced into the top of the cracking tubes, either before or after the balance of the cracking dilution steam has been added to it.
  • the ratio of steam to hydrocarbon employed depends primarily upon the difiioulty encountered in the vaporization of the feedstock, and the coke or tar formation problems encountered in the cracking tubes and subsequent quench and heat recovery units. Normally, the ratio of steam to hydrocarbon feed. employed will range from 0.5 to 3.0 pounds of steam per pound of hydrocarbon. With high boiling feedstooks, the in-line method of fractionation utilizes the cracking dilution steam to reduce the partial pres sure of the hydrocarbon feed, and thereby makes it possible to fractionate or partially vaporize these materials 9 without the use of vacuum stills, or large amounts of other auxiliary steam.
  • the steam reduces the partial pressure of reactants and products Within the cracking tube, and thereby suppresses undesirable secondary reactions which lead to losses of the desired olefinic products such as ethylene, propylene, butadienes, and butylenes.
  • the external temperature of the cracking tube will range from about 1630 F. to 1950 F.
  • the corresponding furnace refractory temperatures will range from about 2000 F. to 2250 F.
  • the cores in relationship to the annuli and size of the tubes are a process variable. They are designed to effeet a balance between the following process requirements: (1) high heat transfer rates and low carbon deposition rates; (2) adequate but minimum residence time for the cracking reaction to be accomplished; and (3) minimum pressure drop consistent with requirement 1) above.
  • the preferred vertical tube arrangement disclosed herein using high temperature alloys is conducive to cleanliness and a minimum of operating problems.
  • the tubes may be varied considerably as to size, being for example, 20 to 80 feet in length and 3 to 16 inches in internal diameter.
  • the advantages of this invention are multifold and include the following: the production of high yields of olefin from a wide variety of basic hydrocarbon feedstocks; the production of cracked gases containing high concentrations of the desired olefinic components; the reduction of energy and investment requirements for the production of olefins; and the minimization of operating problems resulting, for example, from the formation of carbonaceous deposits or from corrosion in the cracking tubes or subsequent cracked gas processing units.
  • (1) means connected with the heat exchangers for passing hydrocarbon and steam therein and therethrough to elfect a vaporized and superheated mixture comprising a first heat exchanger for preheating said hydrocarbon, means for passing said steam and preheated hydrocarbon into a second heat exchanger for vaporizing the said hydrocarbon in the presence of said steam, and means for passing the resulting vapor into a third heat exchanger for superheating the vaporized hydrocarbon-steam mixture, said third heat exchanger having an isolated section thereof with means for passing steam thereinto and therefrom into the bottom portion of the core as superheated steam; and
  • (e) means connected with the third heat exchanger for passing the superheated vaporized hydrocarbon steam mixture therefrom and into the cracking annulus of the furnace.
  • ('b) means connected with the heat exchange apparatus for passing water therethrough to reduce the flue gas temperature and simultaneously generate steam.
  • (f) means connected with the superheat exchanger for passing the superheated mixture therefrom and into the cracking annulus of the furnace.

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  • 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)
US348988A 1964-03-03 1964-03-03 Apparatus for cracking hydrocarbons Expired - Lifetime US3291573A (en)

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Application Number Priority Date Filing Date Title
US348988A US3291573A (en) 1964-03-03 1964-03-03 Apparatus for cracking hydrocarbons
GB31704/64A GB1024005A (en) 1964-03-03 1964-08-04 Improvements in or relating to apparatus and method for cracking hydrocarbons
NL6409295A NL6409295A (US07655688-20100202-C00086.png) 1964-03-03 1964-08-12
ES0304056A ES304056A1 (es) 1964-03-03 1964-09-15 Aparato para el craqueo termico de hidrocarburos normalmente liquidos y normalmente gaseosos en presencia de vapor.
BE653468A BE653468A (US07655688-20100202-C00086.png) 1964-03-03 1965-03-23

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BE (1) BE653468A (US07655688-20100202-C00086.png)
ES (1) ES304056A1 (US07655688-20100202-C00086.png)
GB (1) GB1024005A (US07655688-20100202-C00086.png)
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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3475510A (en) * 1966-04-13 1969-10-28 Lummus Co Ethylene and synthesis gas process
US4426278A (en) 1981-09-08 1984-01-17 The Dow Chemical Company Process and apparatus for thermally cracking hydrocarbons
US4908121A (en) * 1986-05-12 1990-03-13 The M. W. Kellogg Company Flexible feed pyrolysis process
US20040004028A1 (en) * 2002-07-03 2004-01-08 Stell Richard C. Converting mist flow to annular flow in thermal cracking application
US20040004022A1 (en) * 2002-07-03 2004-01-08 Stell Richard C. Process for steam cracking heavy hydrocarbon feedstocks
US20050209495A1 (en) * 2004-03-22 2005-09-22 Mccoy James N Process for steam cracking heavy hydrocarbon feedstocks
US20050261533A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel
US20050261536A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking
US20050261532A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids
US20050261537A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US20050261534A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace
US20050261531A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process and apparatus for cracking hydrocarbon feedstock containing resid
US20050261538A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks
US20050261535A1 (en) * 2004-05-21 2005-11-24 David Beattie Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US20060014993A1 (en) * 2004-07-14 2006-01-19 Stell Richard C Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks
US20060014994A1 (en) * 2004-07-16 2006-01-19 Keusenkothen Paul F Reduction of total sulfur in crude and condensate cracking
US20060014992A1 (en) * 2004-07-14 2006-01-19 Stell Richard C Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks
WO2005113716A3 (en) * 2004-05-21 2006-03-30 Exxonmobil Chem Patents Inc Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace
US20060089519A1 (en) * 2004-05-21 2006-04-27 Stell Richard C Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation
US20060094918A1 (en) * 2004-10-28 2006-05-04 Mccoy James N Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter
US20060129012A1 (en) * 2004-12-10 2006-06-15 Frye James M Vapor/liquid separation apparatus
US7090765B2 (en) 2002-07-03 2006-08-15 Exxonmobil Chemical Patents Inc. Process for cracking hydrocarbon feed with water substitution
US20070004952A1 (en) * 2005-06-30 2007-01-04 Mccoy James N Steam cracking of partially desalted hydrocarbon feedstocks
US20070215524A1 (en) * 2004-05-21 2007-09-20 Stell Richard C Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid

Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
FR2768154A1 (fr) * 1997-09-09 1999-03-12 Procedes Petroliers Petrochim Procede et installation de vapocraquage d'hydrocarbures a charge flexible

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US2230254A (en) * 1937-04-20 1941-02-04 Lavigne Jean Loumiet Et Method for the distillation of liquids
US2304138A (en) * 1939-10-18 1942-12-08 Universal Oil Prod Co Control of simultaneous endothermic and exothermic reactions
US2676156A (en) * 1950-05-19 1954-04-20 Standard Oil Dev Co Preparation of synthesis gas
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US1873454A (en) * 1928-07-12 1932-08-23 Texas Co Method for distilling oils
US2230254A (en) * 1937-04-20 1941-02-04 Lavigne Jean Loumiet Et Method for the distillation of liquids
US2304138A (en) * 1939-10-18 1942-12-08 Universal Oil Prod Co Control of simultaneous endothermic and exothermic reactions
US2676156A (en) * 1950-05-19 1954-04-20 Standard Oil Dev Co Preparation of synthesis gas
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Cited By (67)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3475510A (en) * 1966-04-13 1969-10-28 Lummus Co Ethylene and synthesis gas process
US4426278A (en) 1981-09-08 1984-01-17 The Dow Chemical Company Process and apparatus for thermally cracking hydrocarbons
US4908121A (en) * 1986-05-12 1990-03-13 The M. W. Kellogg Company Flexible feed pyrolysis process
US20040004028A1 (en) * 2002-07-03 2004-01-08 Stell Richard C. Converting mist flow to annular flow in thermal cracking application
US20040004022A1 (en) * 2002-07-03 2004-01-08 Stell Richard C. Process for steam cracking heavy hydrocarbon feedstocks
US7578929B2 (en) 2002-07-03 2009-08-25 Exxonmoil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US7138047B2 (en) 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US20060249428A1 (en) * 2002-07-03 2006-11-09 Stell Richard C Process for steam cracking heavy hydrocarbon feedstocks
US7097758B2 (en) 2002-07-03 2006-08-29 Exxonmobil Chemical Patents Inc. Converting mist flow to annular flow in thermal cracking application
US7090765B2 (en) 2002-07-03 2006-08-15 Exxonmobil Chemical Patents Inc. Process for cracking hydrocarbon feed with water substitution
US7820035B2 (en) 2004-03-22 2010-10-26 Exxonmobilchemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US20050209495A1 (en) * 2004-03-22 2005-09-22 Mccoy James N Process for steam cracking heavy hydrocarbon feedstocks
US20050261535A1 (en) * 2004-05-21 2005-11-24 David Beattie Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7193123B2 (en) 2004-05-21 2007-03-20 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation
US7993435B2 (en) 2004-05-21 2011-08-09 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking hydrocarbon feedstock containing resid
US20050261538A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks
US20050261531A1 (en) * 2004-05-21 2005-11-24 Stell Richard C Process and apparatus for cracking hydrocarbon feedstock containing resid
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US20060089519A1 (en) * 2004-05-21 2006-04-27 Stell Richard C Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation
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BE653468A (US07655688-20100202-C00086.png) 1965-03-23

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