US20090022635A1 - High-performance cracker - Google Patents

High-performance cracker Download PDF

Info

Publication number
US20090022635A1
US20090022635A1 US11/880,189 US88018907A US2009022635A1 US 20090022635 A1 US20090022635 A1 US 20090022635A1 US 88018907 A US88018907 A US 88018907A US 2009022635 A1 US2009022635 A1 US 2009022635A1
Authority
US
United States
Prior art keywords
furnace
section
convection
sub
radiant
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.)
Abandoned
Application number
US11/880,189
Other languages
English (en)
Inventor
Baozhong Zhao
Edward F. Stanley
John R. Garland
Samir J. Serhan
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.)
Linde Engineering North America Inc
Original Assignee
Selas Fluid Processing Corp
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 Selas Fluid Processing Corp filed Critical Selas Fluid Processing Corp
Priority to US11/880,189 priority Critical patent/US20090022635A1/en
Assigned to SELAS FLUID PROCESSING CORPORATION reassignment SELAS FLUID PROCESSING CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ZHAO, BAOZHONG, SERHAN, SAMIR J., GARLAND, JOHN R., STANLEY, EDWARD F.
Priority to PCT/US2008/070152 priority patent/WO2009014949A1/fr
Publication of US20090022635A1 publication Critical patent/US20090022635A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • 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

Definitions

  • the present invention relates to a pyrolytic furnace for cracking hydrocarbon process fluid.
  • the pyrolytic furnace includes multiple convection and radiant sub-sections that are arranged in zones for cracking of hydrocarbon process fluid.
  • pyrolytic furnaces are employed in the petroleum industry to reduce the molecular weight of hydrocarbons by breaking their molecular bonds to yield olefins.
  • cracking of hydrocarbons is a petrochemical process that is widely used to produce olefins such as ethylene, propylene, butenes, butadiene, from a hydrocarbon feedstock such as naphtha, ethane, propane, gas oil or other fractions of whole crude oil.
  • the cracking process is commonly carried out in a pyrolytic furnace (also referred to herein as a cracker or steam cracker). The process may also be carried out in a heater, boiler, kiln, or kettle. Pyrolytic furnaces generally include a convection section and a radiant section.
  • a hydrocarbon process fluid is first delivered into the convection section of the pyrolytic furnace, whereupon the hydrocarbon process fluid is preheated and diluted with steam.
  • the preheated and diluted hydrocarbon process fluid is then delivered into the higher temperature radiant section, where cracking of the hydrocarbon process fluid occurs, yielding olefins.
  • the resulting olefins are available for consumption, distribution or storage.
  • a conventional pyrolytic furnace is illustrated in U.S. Patent Application Publication No. 2003/0209469 to Kivlen, for example, which is incorporated by reference herein in its entirety.
  • the hydrocarbon cracking process begins by supplying a hydrocarbon feedstock to a furnace.
  • the hydrocarbon feedstock is mixed with steam, which serves as a diluent to keep the hydrocarbon molecules separated.
  • the hydrocarbon feedstock mixture is preheated in the convection section by flue gas from the burners positioned in the radiant section of the furnace. Once the hydrocarbon feedstock has been preheated, the feedstock is transferred to the radiant section of the furnace.
  • the radiant section contains a plurality of radiant tubes through which the preheated hydrocarbon feedstock is distributed.
  • the radiant section also contains a plurality of heat sources that supply the heat that is necessary for cracking the preheated hydrocarbon feedstock contained within the radiant tubes.
  • coke carbon deposits
  • This phenomena is commonly referred to in the art as coking.
  • Coke tends to reduce the heat exchange efficiency between the heat sources and the hydrocarbon feed within radiant coils, necessitating a greater quantity of thermal energy to crack the hydrocarbon feed within each radiant coil, consequently increasing the tube wall temperature and the process side pressure drop.
  • the build-up of coke may vary from coil to coil, as the combustion heat may fluctuate from heat source to heat source, or the inner diameter, surface roughness or surface profile of each coil may also vary.
  • the radiant coils must be decoked in order to restore the efficiency of the furnace, and to maintain the tube metal temperature below its maximum permissible design temperature and also to maintain the process side pressure drop within design limits.
  • Decoking is the process of removing carbon deposits from the interior walls of the radiant coils, and is part of routine maintenance in an effort to maintain high-efficiency of a pyrolytic furnace and safe operation. Furnaces may be decoked by distributing air and steam through the radiant coils, for example.
  • the entire pyrolytic furnace is off-line during the decoking cycle. Unscheduled or frequent decoking cycles may lead to a reduction in olefin production, shortened radiant tube life, and higher furnace maintenance costs.
  • On-line decoking is not a realistic option for many conventional furnaces, however. Specifically, all of the radiant coils and the convection coils of conventional furnaces, such as the one disclosed in the Kivlen publication, are maintained at substantially the same temperature, by virtue of the relative arrangement of their convection coils, radiant coils and burners. In contrast, in an on-line decoking cycle, the radiant coils being decoked require less heat input than the radiant coils carrying the hydrocarbon feed. Reducing the heat emitted by the heat sources to achieve decoking in some coils, consequently decreases the heat within the radiant section to a level insufficient for cracking the hydrocarbon feed within the other radiant coils at the design flow rate.
  • pyrolytic furnaces In an effort to achieve benefits such as on-line decoking, pyrolytic furnaces have been developed including plural radiant sections. Each radiant section receives hydrocarbon feed from a common convection section. Such a pyrolytic furnace may be referred to in the art as having a ‘twin radiant box’ or ‘twin radiant cell’ design. In an on-line decoking cycle, one radiant box undergoes decoking, while the other radiant box undergoes cracking. However, because one radiant box is decoking and therefore off-line for production, the furnace is only operating at 50% efficiency.
  • the invention relates to a pyrolytic furnace for thermally cracking hydrocarbon process fluid, and a method of operating the pyrolytic furnace.
  • the furnace comprises a convection section including a plurality of convection sub-sections, a radiant section comprising a plurality of radiant sub-sections, and an enclosure defining a plurality of discrete sectors.
  • Each discrete sector of the enclosure includes a convection sub-section having at least one convection conduit for carrying hydrocarbon process fluid, at least one radiant sub-section having at least one radiant conduit connected to receive preheated hydrocarbon process fluid from the convection conduit, and a heat source configured to deliver heat into the discrete sector. Adjacent sectors of the furnace are segregated from each other, such that the heat delivered from the heat source is substantially localized in the discrete sector of the enclosure.
  • each convection conduit is contained entirely within its respective convection sub-section.
  • a method of operating a pyrolytic furnace comprises the step of distributing hydrocarbon process fluid into a convection section of a discrete sector of the furnace.
  • the pre-heated hydrocarbon process fluid is transferred from the convection section of the discrete sector into at least one corresponding radiant section of the discrete sector.
  • Heat is delivered into the at least one radiant section of the discrete sector of the furnace to crack the pre-heated hydrocarbon process fluid, wherein the heat is substantially concentrated in the discrete sector of the furnace.
  • FIG. 1 is a front elevation schematic view of an exemplary pyrolytic furnace
  • FIG. 2A is a front elevation schematic view of a pyrolytic furnace according to an exemplary embodiment of the invention.
  • FIG. 2B is a perspective view of a single radiant box arrangement of the pyrolytic furnace of FIG. 2A shown schematically;
  • FIG. 2C is a perspective view of another pyrolytic furnace having a single radiant box arrangement shown schematically;
  • FIG. 2D is a right side elevation schematic view illustrating a twin radiant box arrangement of the pyrolytic furnace of FIG. 2A ;
  • FIGS. 3-5 are front elevation schematic views of various pyrolytic furnaces according to exemplary embodiments of the invention.
  • FIG. 6 is a perspective view of a convection section of a furnace shown schematically (radiant section omitted) according to an exemplary embodiment of the invention.
  • FIG. 7 is a perspective view of another convection section of a furnace shown schematically (radiant section omitted) according to an exemplary embodiment of the invention.
  • a furnace 200 , 300 , 400 , 500 comprises a convection section 210 , 310 , 410 , and 510 including a plurality of convection sub-sections 210 (A-D), 310 (A-D), 410 (A-D), and 510 (A-D) a radiant section 250 , 350 , 450 , and 550 comprising a plurality of radiant sub-sections 250 (A-D), 350 (A-D), 450 (A-D), and 550 (A-D) and an enclosure 212 , 312 , 412 and 512 defining a plurality of discrete sectors.
  • Each discrete sector of the enclosure includes a convection sub-section 210 (A-D), 310 (A-D), 410 (A-D), and 510 (A-D) having at least one convection conduit for carrying hydrocarbon process fluid, at least one radiant sub-section 250 (A-D), 350 (A-D), 450 (A-D) and 550 (A-D) having at least one radiant conduit connected to receive preheated hydrocarbon process fluid from the convection conduit, and a heat source 230 , 330 , 430 , 530 configured to deliver heat into the discrete sector. Adjacent sectors of the furnace 200 , 300 , 400 and 500 are segregated from each other, such that the heat delivered from the heat source is substantially localized in the discrete sector of the enclosure 212 , 312 , 412 and 512 .
  • the pyrolytic furnace 100 includes a convection section 110 for preheating and diluting hydrocarbon feed 132 , and a radiant section 150 for cracking the hydrocarbon feed to yield effluent 136 comprising olefins and byproducts.
  • the convection section 110 of the furnace 100 includes two sets of coils 114 and 122 positioned within an enclosure 112 of the furnace. The coils 114 and 122 extend along the entire length “L” of the convection section 110 .
  • the hydrocarbon feed 132 goes through two sections of convection section 110 .
  • the hydrocarbon feed 132 is distributed through feed preheat coils 114 that extend along the entire length “L” of the convection section 110 .
  • the preheated hydrocarbon feed 132 is then distributed through a set of conduits 140 (four shown) positioned exterior to the enclosure 112 . Steam is injected into each conduit 140 for diluting the preheated hydrocarbon feed 132 .
  • Conduits interconnecting the preheat coils, such as conduit 140 may also be referred to in the art as ‘jumpovers.’
  • the diluted and preheated hydrocarbon feed is distributed through the mix-feed preheat coils 122 that extend along the entire length “L” of the convection section 110 .
  • the term ‘mix’ refers to the mixing that occurs between the hydrocarbon feed and the steam within the coils 122 .
  • the coils 114 and 122 are heated by thermal energy generated by a heat source 130 positioned within the radiant section 150 . Thermal energy emitted by the heat source 130 rises through the radiant section 150 and into the convection section 110 , consequently heating the hydrocarbon feed within the coils 114 and 122 .
  • the individual diluted and preheated hydrocarbon feed streams are then transported through individual conduits 126 into the radiant section 150 .
  • Conduits interconnecting the convection section with the radiant section, such as conduits 126 may also be referred to in the art as ‘crossovers.’
  • the diluted and preheated hydrocarbon feed streams are then distributed through a series of radiant coils 128 extending along the height “H” of the radiant section 150 .
  • the diluted and preheated hydrocarbon feed streams are heated within the radiant coils 128 by the heat source 130 .
  • the hydrocarbon feed is heated to a temperature of above 1200 degrees Fahrenheit, for example, which is sufficient to crack the hydrocarbon mixture and yield effluent 136 .
  • FIGS. 2A and 2B front and perspective views of another pyrolytic furnace 200 are illustrated schematically, according to an exemplary embodiment of the invention.
  • the furnace 200 includes a convection section 210 for preheating a diluting hydrocarbon feed stock 232 and a radiant section 250 for cracking the hydrocarbon feed stock to yield effluent 236 comprising olefins and byproducts.
  • the convection and radiant sections are optionally contained within a single enclosure 212 .
  • the convection section 210 includes a plurality of convection sub-sections 210 (A), 210 (B), 210 (C) and 210 (D), collectively referred to as 210 (A-D). Only convection sub-section 210 (D) is illustrated in FIG. 2B for clarity.
  • the radiant section 250 optionally comprises four radiant sub-sections 250 (A), 250 (B), 250 (C) and 250 (D), collectively referred to as item 250 (A-D). Only radiant sub-section 250 (D) is illustrated in FIG. 2B for clarity.
  • the sub-sections of the convection and radiant sections are preferably organized in sectors within the enclosure 212 .
  • the furnace 200 shown in FIG. 2A includes four sectors.
  • Each sector includes a convection sub-section 210 (A-D), a corresponding radiant sub-section 250 (A-D), and a set of heat sources 230 (8 per sector).
  • the first sector comprises convection sub-section 210 (A), radiant sub-section 250 (A) and 8 heat sources 230 .
  • the second sector comprises convection sub-section 210 (B), radiant sub-section 250 (B) and 8 heat sources 230 , and so forth.
  • Each convection sub-section 210 is configured to preheat and dilute the hydrocarbon feed 232 for distribution into a corresponding radiant sub-section 250 (A-D).
  • the convection sub-sections 210 (A-D) optionally comprises a feed preheat section 214 and a mix-feed preheat section 222 .
  • Each coil is a thermally conductive hollow tube capable of carrying hydrocarbon feed. The individual coils are preferably positioned within the boundaries of their respective sector, the significance of which will be explained in greater detail below.
  • hydrocarbon feed 232 is first distributed through the feed preheat section 214 of each sector.
  • Each feed preheat section 214 is heated by a set of heat sources 230 positioned with its respective sector.
  • the pre-heated hydrocarbon feed 232 is then delivered into a series of individual conduits 240 (three conduits per sub-section shown). As shown in FIG. 2B , the individual conduits 240 optionally extend outside of the enclosure 212 .
  • Steam 234 is then delivered into each conduit 240 through an inlet port (not shown). The steam 234 dilutes the preheated hydrocarbon feed within the conduits 240 .
  • the diluted and pre-heated hydrocarbon feed is thereafter distributed through the mix-feed preheat section 222 of each convection sub-section 210 (A-D) for further heating.
  • the diluted and twice pre-heated hydrocarbon feed is then distributed through a series of individual conduits 226 (three conduits shown) and into respective sub-sections of the radiant section 250 .
  • the individual conduits 226 optionally extend outside of the enclosure 212 .
  • Each radiant sub-section 250 comprises a plurality of radiant coils 228 , and a set of heat sources 230 (8 heat sources per sector).
  • Each radiant coil 228 is a thermally conductive hollow tube through which the hydrocarbon feed is distributed. The radiant coils 228 are heated by heat sources 230 for cracking the hydrocarbon feed within each coil 228 to yield effluent 236 .
  • the discrete sectors are oriented in a side-by-side arrangement along the length “L” of the furnace 200 , whereby adjacent convection and radiant sub-sections are each separated by a gap “G.”
  • the gap “G” may be about two times as large as the outer diameter of a conduit 228 . Accordingly, no conduit or coil of a convection sub-section 210 (A-D) or a radiant sub-section 250 (A-D) overlaps or intrudes upon the space boundaries of an adjacent sector.
  • heat generated by each set of heat sources 230 is substantially concentrated in that sector.
  • heat emitted by the heat sources 230 of the first sector provides heat to radiant sub-section 250 (A) and convection sub-section 210 (A), and so forth.
  • heat may radiate into an adjacent sector regardless of the gap “G.”.
  • the heat generated by each set of heat sources 230 may be adjusted for controlling the temperature of each sector.
  • the radiant coils carrying hot steam and air i.e., undergoing decoking
  • the furnace 200 may include provisions such that its length “L” may be increased to accommodate a greater number of sectors (each sector including at least one radiant sub-section and a corresponding convection sub-section).
  • the furnace 200 is also uniquely adapted to maximize the olefin yields of each sector.
  • the flow rate and/or the temperature of a single sector may be adjusted without adversely impacting the temperature of an adjacent sector to a significant degree.
  • the olefin yields may be maximized for each sector of the furnace.
  • Segregating the convection and radiant section of the furnace into sectors may be particularly advantageous if hydrocarbon feeds 232 of varying compositions (i.e., hydrocarbon feeds having varied cracking temperatures) are distributed through different sectors of the furnace 200 .
  • the temperature of each sector may be tailored for the hydrocarbon feed distributed therethrough.
  • olefin yields of conventional furnaces vary from radiant coil to radiant coil. Adjusting the flow rate and/or temperature of a single radiant coil to maximize the olefin yield of the hydrocarbon feed within one coil may adversely impact the temperature of an adjacent radiant coil. Thus, adjustment of either the flow rate and/or temperature of a single hydrocarbon stream is limited by the temperature constraints of the adjacent hydrocarbon streams. Once the temperature variation between the radiant coils becomes too great, the conventional furnace would be off-line for early non-routine maintenance, which is undesirable from the operational and cost perspectives.
  • each hydrocarbon stream 232 is consecutively distributed through a coil of feed preheat section 214 , a conduit 240 , a coil of mix-feed preheat section 222 , a conduit 226 and a radiant coil 228 .
  • the individual hydrocarbon streams 232 of each sub-section combined.
  • the individual hydrocarbon streams may be combined together at one or more junctions to promote even heating and dilution of the hydrocarbon feed.
  • FIG. 2C depicts an alternative exemplary embodiment of the invention.
  • Furnace 200 ′ is similar to furnace 200 of FIGS. 2A and 2B , with the exception of the manifold 226 ′ and the modified radiant coils 228 ′.
  • three individual hydrocarbon feed streams are combined in a manifold 226 ′ after the hydrocarbon feed is distributed through the mix-feed preheat section 222 of each convection sub-section 210 (A-D).
  • the manifold 226 ′ promotes even heating and dilution of the hydrocarbon feed streams 232 .
  • the manifold 226 ′ optionally extends outside of the enclosure 212 . Although only one sector of the furnace 200 ′ is shown in FIG. 2C , it should be understood that each sector of the furnace 200 ′ may include a manifold 226 ′.
  • the radiant coils 228 ′ differ from the radiant coils shown in FIGS. 2A and 2B , in that the radiant coils 228 ′ are “U”-shaped. Thus, instead of distributing the effluent 236 at the bottom of the enclosure 212 , the radiant coils 228 ′ distribute the effluent 236 at an elevation above the radiant sub-sections 250 (A-D).
  • FIGS. 2B and 2C indicate that furnaces 200 and 200 ′ have a single radiant box arrangement, i.e., one radiant sub-section corresponding to one convection sub-section.
  • the furnace 200 ′′ encompasses a twin radiant box arrangement, i.e., two radiant sub-sections corresponding to each convection sub-section.
  • FIG. 2D depicts a right side elevation schematic view of a twin radiant box furnace 200 ′′ having two radiant sub-sections corresponding to each convection sub-section. Specifically, FIG. 2D depicts one sector of furnace 200 ′′ that includes two radiant sub-sections 250 (D′′) and 250 (E) corresponding to one convection sub-section 210 (D′′). Each radiant sub-section includes one or more heat sources 230 for heating the hydrocarbon feed. It should be understood that the furnace 200 ′′ optionally includes four (4) convection sub-sections and eight (8) radiant sub-sections.
  • Each convection sub-section of furnace 200 ′′ comprises a feed preheat section 214 ′′ and a mix-feed preheat section 222 ′′.
  • the feed preheat section 214 ′′ and the mix-feed preheat section 222 ′′ may optionally include two times the number of coils as the convection section of FIG. 2A , because each feed and mix-feed preheat section 214 ′′ and 222 ′′ supplies hydrocarbon feed to twice the number of radiant sub-sections.
  • hydrocarbon feed 232 is first distributed through the feed preheat section 214 ′′ of each sector.
  • the pre-heated hydrocarbon feed 232 is then delivered into a series of individual conduits 240 .
  • Steam 234 is then delivered into each conduit 240 through an inlet port (not shown).
  • the diluted and pre-heated hydrocarbon feed is thereafter distributed through the mix-feed preheat section 222 ′′ of each convection sub-section for further heating.
  • the diluted and twice pre-heated hydrocarbon feed is then distributed through a series of individual conduits 226 and into the “U”-shaped radiant coils 228 ′′ of respective radiant sub-sections 250 (D′′) and 250 (E).
  • the effluent is then distributed from the “U”-shaped radiant coils 228 ′′ at an elevation above the radiant sub-sections 250 (D′′) and 250 (E).
  • each convection sub-section 310 includes a manifold 340 interconnecting the feed preheat section 314 with the mix-feed preheat section 322 .
  • the hydrocarbon feed streams 332 (five shown) combine together in the manifolds 340 .
  • Steam 334 is injected into each manifold 340 at an inlet port (not shown) for mixing with the combined hydrocarbon feed streams 332 .
  • Each convection sub-section 310 (A-D) also includes a manifold 326 interconnecting the mix-feed preheat section 322 with the radiant coils 328 .
  • the manifolds 326 and 340 promote even heating and dilution of the hydrocarbon feed streams 332 .
  • the build-up of coke may vary from coil to coil, consequently affecting the flow rate and temperature of each hydrocarbon feed stream.
  • combining the hydrocarbon feed streams 332 of each convection sub-section 310 (A-D) at one or more locations promotes even heating and dilutions of the hydrocarbon feed streams.
  • FIG. 4 another exemplary embodiment of a pyrolytic furnace 400 is shown.
  • the pyrolytic furnace 400 is similar to the furnace 200 shown in FIG. 2A , with the exception that each convection sub-section 410 (A-D) includes an additional mix-feed preheat section 423 and steam injection point 435 .
  • the additional mix-feed preheat section 423 and steam injection points 435 meet special process requirements of heavy feed stock.
  • the individual conduits 440 , 441 and 426 extending between the feed preheat sections 414 , 423 and 422 may be replaced by manifolds, similar to the manifolds shown in FIG. 3 , to promote even heating of the hydrocarbon feed streams 432 .
  • the pyrolytic furnace 500 is similar to the furnace 200 shown in FIG. 2A , however, the furnace 500 includes insulating partitions 564 , 566 and 560 positioned between adjacent sectors of the furnace. Specifically, partitions 564 are positioned between adjacent feed preheat sub-sections 514 , partitions 566 are positioned between adjacent mix-feed preheat sub-sections 522 , and partitions 560 are positioned between adjacent radiant sub-sections 550 (A-D).
  • partitions 564 are positioned between adjacent feed preheat sub-sections 514
  • partitions 566 are positioned between adjacent mix-feed preheat sub-sections 522
  • partitions 560 are positioned between adjacent radiant sub-sections 550 (A-D).
  • Each partition 560 extends upwards from the base 562 of the enclosure 512 for shielding adjacent radiant sub-sections 550 (A-D).
  • the partitions 560 may extend along a portion of the height of the radiant section (as shown), or, alternatively, the partitions 560 may extend along the entire height of the radiant section 550 . Also, although not shown, the partitions 560 may optionally be suspended from the roof 570 of the radiant section 550 to achieve a similar effect.
  • each sector of the furnace optionally includes a series of flue gas shutters 572 positioned between each convection sub-section, e.g., 510 (A), and its corresponding radiant section e.g., 550 (A).
  • the flue gas shutters 572 are moveable to control the amount of heat delivered to each convection sub-section 510 (A-D).
  • one or more feed preheat coils may be positioned across the entire length “L” of the convection section, as shown in FIG. 6 .
  • FIG. 6 a schematic perspective view of a convection section 610 is shown according to an exemplary embodiment of the invention.
  • the radiant section of the furnace has been omitted.
  • the convection section 610 is similar to the convection section 310 of the furnace 300 shown in FIG. 3 , however the feed preheat sections 314 of FIG. 3 are replaced by four stream feed preheat coils 614 ( 1 ), 614 ( 2 ), 614 ( 3 ), and 614 ( 4 ), referred to as 614 collectively.
  • the feed preheat coils 614 are staggered along the width “W” of the interior of the enclosure 612 .
  • Each feed preheat coil 614 includes five 180 degree bends such that each coil 614 traverses the entire length “L” of the enclosure 612 six times.
  • the convection section 610 may include any number of preheat coils, and each preheat coil may be configured to traverse the length “L” of the enclosure 612 any number of times.
  • the convection section 610 further comprises four mix-feed preheat sections 622 (A-D) staggered along the length “L” of the interior of the enclosure 612 .
  • the mix-feed preheat sections 622 (A-D) are substantially equivalent to mix-feed preheat sections 322 of FIG. 3 . Accordingly, the individual coils 625 of each mix-feed preheat sections 622 (A-D) traverse the width of the enclosure 612 .
  • the mix-feed preheat sections 622 (A-D) are fluidly coupled to the feed preheat coils 614 by a manifold 640 . Although not shown, manifold 640 may be replaced by individual conduits, if so desired.
  • each mix-feed preheat section 622 (A-D) is fluidly coupled to another manifold 626 .
  • Each manifold 626 is fluidly coupled to two (2) radiant conduits 628 .
  • the radiant conduits 628 extend into a corresponding radiant sub-section (not shown).
  • hydrocarbon feed 632 is delivered through a manifold 613 into feed preheat coils 614 .
  • the hydrocarbon feed 632 is then delivered into a manifold 640 where all four hydrocarbon feed streams are combined together and mixed with steam 634 .
  • Combining the hydrocarbon feed streams into a common manifold 640 promotes even dilution and heating of the hydrocarbon feed.
  • the diluted hydrocarbon feed stream is then delivered into four mix-feed preheat sub-sections 622 (A-D).
  • the diluted hydrocarbon feed stream is pre-heated within each coil 625 of the mix-feed preheat sub-sections 622 (A-D) by heat sources (not shown).
  • the twice-preheated and diluted hydrocarbon feed streams 624 are delivered into a respective manifold 626 , where the streams are combined together and optionally mixed with steam (not shown).
  • the hydrocarbon feed within each manifold 626 is then distributed into two radiant conduits 626 and delivered into a corresponding radiant sub-section (not shown) for cracking.
  • the convection section 710 is similar to the convection section 610 shown in FIG. 6 , with the exception that convection section 710 includes two feed preheat sections 714 and 723 extending across the length “L” of the enclosure 712 instead of one feed preheat section. More particularly, the convection section 710 comprises four additional feed pre-heat coils 723 ( 1 ), 723 ( 2 ), 723 ( 3 ), and 723 ( 4 ), referred to herein as 723 collectively. Each feed preheat coil 723 includes three 180 degree bends such that each coil 723 traverses the entire length “L” of the enclosure 712 four times. The coil 723 can be used as a feed preheat coil or a mixed feed preheat coil.
  • the convection section 710 also includes four mix-feed preheat sections 722 (A-D) staggered along the length “L” of the interior of the enclosure 712 .
  • the mix-feed preheat sections 722 are fluidly coupled to the feed preheat coils 714 by a manifold 741 .
  • each mix-feed preheat section 722 is fluidly coupled to another manifold 726 .
  • Each manifold 726 is fluidly coupled to two (2) radiant conduits 728 .
  • the radiant conduits 728 extend into a corresponding radiant sub-section (not shown).
  • hydrocarbon feed 732 is delivered through a manifold 713 into four feed preheat coils 714 staggered along the length of the enclosure. After traveling through the coils 714 , the hydrocarbon feed 732 is then delivered into a manifold 740 where all four hydrocarbon feed streams are combined together and mixed with steam 734 . The diluted hydrocarbon feed is then distributed through four mix-feed preheat coils 723 and delivered into a manifold 741 where all four hydrocarbon feed streams are combined together and mixed with steam 735 again. The twice-diluted hydrocarbon feed is then delivered into four mix-feed preheat sub-sections 722 (A-D).
  • the mix-feed preheat sub-sections 722 (A-D) are substantially equivalent to the mix-feed preheat sub-sections 622 (A-D) of FIG. 6 , and no further explanation is required.
  • the manifolds 713 , 740 and 735 may be replaced by individual conduits, if so desired.
  • exemplary embodiments of this invention provide high capacity pyrolytic furnaces that can meet the rapidly expanding global demand for ethylene.
  • the radiant coil length and the number of radiant coils may be increased, resulting in a larger radiant enclosure.
  • expansion of the radiant section is not constrained by limitations of the convection section.
  • the number and size of convection conduits or coils should preferably increase as the number and size of radiant conduits or coils increase.
  • the number and size of convection conduits or coils can optionally be increased (or decreased) along with the number of radiant conduits or coils.
  • This additional benefit conferred by exemplary embodiments of this invention can be incorporated to avoid several disadvantages.
  • independently increasing the length of convection conduits or coils (without changing their number) may result in excessive thermal expansion and/or a high pressure drop.
  • independently increasing the width “W” (see FIG. 1 ) of the convection section enclosure to accommodate a greater number of convection conduits or coils typically would require additional mechanical supports for retaining all of the additional convection conduits or coils, at an added expense, which would reach economical design limits. Accordingly, these additional disadvantages can be overcome by exemplary embodiments of this invention, which allow for enlarging the capacity of the furnace.
  • the convection and radiant sections may include any number of coils and conduits.
  • each sector may include any number of heat sources, convection sub-sections, or radiant sub-sections to meet any desired purpose.

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)
US11/880,189 2007-07-20 2007-07-20 High-performance cracker Abandoned US20090022635A1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US11/880,189 US20090022635A1 (en) 2007-07-20 2007-07-20 High-performance cracker
PCT/US2008/070152 WO2009014949A1 (fr) 2007-07-20 2008-07-16 Craqueur à haute performance

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US11/880,189 US20090022635A1 (en) 2007-07-20 2007-07-20 High-performance cracker

Publications (1)

Publication Number Publication Date
US20090022635A1 true US20090022635A1 (en) 2009-01-22

Family

ID=40264988

Family Applications (1)

Application Number Title Priority Date Filing Date
US11/880,189 Abandoned US20090022635A1 (en) 2007-07-20 2007-07-20 High-performance cracker

Country Status (2)

Country Link
US (1) US20090022635A1 (fr)
WO (1) WO2009014949A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102041031A (zh) * 2010-12-17 2011-05-04 惠生工程（中国）有限公司 乙烯裂解炉用穿膛柱结构及其制造方法
US20220119716A1 (en) * 2020-10-15 2022-04-21 Technip Process Technology, Inc. Hybrid ethylene cracking furnace
WO2022225691A1 (fr) * 2021-04-19 2022-10-27 Exxonmobil Chemical Patents Inc. Procédés et systèmes de vapocraquage de charges hydrocarbonées

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103992812B (zh) * 2014-05-28 2016-04-06 惠生工程（中国）有限公司 乙烯裂解炉

Citations (57)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2121209A (en) * 1933-04-19 1938-06-21 Gasoline Prod Co Inc Treatment of hydrocarbon oil
US2263557A (en) * 1937-12-30 1941-11-25 Du Pont Conversion of hydrocarbons
US3671198A (en) * 1970-06-15 1972-06-20 Pullman Inc Cracking furnace having thin straight single pass reaction tubes
US3841274A (en) * 1973-11-29 1974-10-15 Universal Oil Prod Co High temperature heater for fluids
US4291669A (en) * 1979-06-25 1981-09-29 Herne Jr Robert H Efficient fuel burning stove or furnace with thermal energy slow propagation flue structure
US4342642A (en) * 1978-05-30 1982-08-03 The Lummus Company Steam pyrolysis of hydrocarbons
US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process
US4499055A (en) * 1981-09-14 1985-02-12 Exxon Research & Engineering Co. Furnace having bent/single-pass tubes
US4617109A (en) * 1985-12-23 1986-10-14 The M. W. Kellogg Company Combustion air preheating
US4732740A (en) * 1984-10-09 1988-03-22 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process
US4765883A (en) * 1982-10-20 1988-08-23 Stone & Webster Engineering Corporation Process for the production of aromatics benzene, toluene, xylene (BTX) from heavy hydrocarbons
US4780196A (en) * 1985-07-12 1988-10-25 Institut Francais Du Petrole Hydrocarbon steam cracking method
US4906442A (en) * 1982-09-30 1990-03-06 Stone & Webster Engineering Corporation Process and apparatus for the production of olefins from both heavy and light hydrocarbons
US4908121A (en) * 1986-05-12 1990-03-13 The M. W. Kellogg Company Flexible feed pyrolysis process
US4940828A (en) * 1989-10-13 1990-07-10 The M. W. Kellogg Company Steam cracking feed gas saturation
US5124003A (en) * 1986-06-25 1992-06-23 Naphtachimie S.A. Apparatus for the steam cracking of hydrocarbons for the preparation of olefins an diolefins
US5151158A (en) * 1991-07-16 1992-09-29 Stone & Webster Engineering Corporation Thermal cracking furnace
US5181990A (en) * 1986-01-16 1993-01-26 Babcock-Hitachi Kabushiki Kaisha Pyrolysis furnace for olefin production
US5190634A (en) * 1988-12-02 1993-03-02 Lummus Crest Inc. Inhibition of coke formation during vaporization of heavy hydrocarbons
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5271809A (en) * 1991-08-28 1993-12-21 Selas-Kirchner Gmbh Pyrolytic furnace for the thermal cracking of hydrocarbons
US5271827A (en) * 1990-11-29 1993-12-21 Stone & Webster Engineering Corp. Process for pyrolysis of hydrocarbons
US5358626A (en) * 1993-08-06 1994-10-25 Tetra International, Inc. Method for retarding corrosion and coke formation and deposition during pyrolytic hydrocarbon procssing
US5364995A (en) * 1991-03-05 1994-11-15 Bp Chemicals Limited Polymer cracking
US5372706A (en) * 1993-03-01 1994-12-13 Mobil Oil Corporation FCC regeneration process with low NOx CO boiler
US5389342A (en) * 1991-12-30 1995-02-14 Pillips Petroleum Company Apparatus for dehydrogenation process control
US5446229A (en) * 1992-12-18 1995-08-29 Amoco Corporation Thermal cracking process with reduced coking
US5866745A (en) * 1998-01-26 1999-02-02 Abb Lummus Global Inc. Catalytic/oxidative promoted hydrocarbon pyrolysis
US5972206A (en) * 1994-12-26 1999-10-26 Institut Francais Du Petrole Flexible steam cracking process and corresponding steam cracking facility
US5981818A (en) * 1995-03-21 1999-11-09 Stone & Webster Engineering Corp. Integrated cracking and olefins derivative process utilizing dilute olefins
US6013852A (en) * 1997-11-21 2000-01-11 Shell Oil Company Producing light olefins from a contaminated liquid hydrocarbon stream by means of thermal cracking
US6027635A (en) * 1995-12-27 2000-02-22 Institute Francais Du Petrole Continuous pyrolysis and decoking process for use in the production of acetylene
US6168709B1 (en) * 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US6228253B1 (en) * 1997-06-05 2001-05-08 Zalman Gandman Method for removing and suppressing coke formation during pyrolysis
US6312652B1 (en) * 1997-09-19 2001-11-06 Stone & Webster Engineering Corp. Ceramic dip pipe and tube reactor for ethylene production
US6425757B1 (en) * 2001-06-13 2002-07-30 Abb Lummus Global Inc. Pyrolysis heater with paired burner zoned firing system
US6464858B1 (en) * 1994-08-25 2002-10-15 Phillips Petroleum Company Method for improving the yield of heavy hydrocarbons in a thermal cracking process
US20030070962A1 (en) * 2001-09-19 2003-04-17 Qingquan Zeng Pyrolysis furnace with new type radiant tubes arrangement and method of its operation and usage
US6632351B1 (en) * 2000-03-08 2003-10-14 Shell Oil Company Thermal cracking of crude oil and crude oil fractions containing pitch in an ethylene furnace
US20030209469A1 (en) * 2002-05-07 2003-11-13 Westlake Technology Corporation Cracking of hydrocarbons
US20030213687A1 (en) * 2002-04-10 2003-11-20 Platvoet Erwin M.J. Cracking furnace with more uniform heating
US6685893B2 (en) * 2001-04-24 2004-02-03 Abb Lummus Global Inc. Pyrolysis heater
US6706246B2 (en) * 2001-02-26 2004-03-16 Abb Lummus Global Inc. System and method for the selective catalytic reduction of nitrogen oxide in a gas stream
US6719953B2 (en) * 1997-06-10 2004-04-13 Exxonmobil Chemical Patents Inc. Process for the manufacture of olefins by a pyrolysis furnace with an internally finned U shaped radiant coil
US6743961B2 (en) * 2002-08-26 2004-06-01 Equistar Chemicals, Lp Olefin production utilizing whole crude oil
US20040147794A1 (en) * 2003-01-24 2004-07-29 Brown David J. Process for cracking hydrocarbons using improved furnace reactor tubes
US6852294B2 (en) * 2001-06-01 2005-02-08 Conocophillips Company Alternate coke furnace tube arrangement
US20050176831A1 (en) * 2004-01-09 2005-08-11 Taiji Inui Steam reforming system
US20050209495A1 (en) * 2004-03-22 2005-09-22 Mccoy James N Process for steam cracking heavy hydrocarbon feedstocks
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
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
US6979757B2 (en) * 2003-07-10 2005-12-27 Equistar Chemicals, Lp Olefin production utilizing whole crude oil and mild controlled cavitation assisted cracking
US20060045828A1 (en) * 2004-09-01 2006-03-02 Aaron Timothy M Catalytic reactor
US7019187B2 (en) * 2002-09-16 2006-03-28 Equistar Chemicals, Lp Olefin production utilizing whole crude oil and mild catalytic cracking
US7090013B2 (en) * 2001-10-24 2006-08-15 Shell Oil Company In situ thermal processing of a hydrocarbon containing formation to produce heated fluids
US7125483B2 (en) * 2003-04-10 2006-10-24 Equistar Chemicals, Lp Corrosion control in olefin production plants
US7138047B2 (en) * 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2748273B1 (fr) * 1996-05-06 1998-06-26 Inst Francais Du Petrole Procede et dispositif de conversion thermique d'hydrocarbures en hydrocarbures aliphatiques plus insatures que les produits de depart, combinant une etape de vapocraquage et une etape de pyrolyse

Patent Citations (57)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2121209A (en) * 1933-04-19 1938-06-21 Gasoline Prod Co Inc Treatment of hydrocarbon oil
US2263557A (en) * 1937-12-30 1941-11-25 Du Pont Conversion of hydrocarbons
US3671198A (en) * 1970-06-15 1972-06-20 Pullman Inc Cracking furnace having thin straight single pass reaction tubes
US3841274A (en) * 1973-11-29 1974-10-15 Universal Oil Prod Co High temperature heater for fluids
US4342642A (en) * 1978-05-30 1982-08-03 The Lummus Company Steam pyrolysis of hydrocarbons
US4291669A (en) * 1979-06-25 1981-09-29 Herne Jr Robert H Efficient fuel burning stove or furnace with thermal energy slow propagation flue structure
US4499055A (en) * 1981-09-14 1985-02-12 Exxon Research & Engineering Co. Furnace having bent/single-pass tubes
US4906442A (en) * 1982-09-30 1990-03-06 Stone & Webster Engineering Corporation Process and apparatus for the production of olefins from both heavy and light hydrocarbons
US4765883A (en) * 1982-10-20 1988-08-23 Stone & Webster Engineering Corporation Process for the production of aromatics benzene, toluene, xylene (BTX) from heavy hydrocarbons
US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process
US4732740A (en) * 1984-10-09 1988-03-22 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process
US4780196A (en) * 1985-07-12 1988-10-25 Institut Francais Du Petrole Hydrocarbon steam cracking method
US4617109A (en) * 1985-12-23 1986-10-14 The M. W. Kellogg Company Combustion air preheating
US5181990A (en) * 1986-01-16 1993-01-26 Babcock-Hitachi Kabushiki Kaisha Pyrolysis furnace for olefin production
US4908121A (en) * 1986-05-12 1990-03-13 The M. W. Kellogg Company Flexible feed pyrolysis process
US5124003A (en) * 1986-06-25 1992-06-23 Naphtachimie S.A. Apparatus for the steam cracking of hydrocarbons for the preparation of olefins an diolefins
US5190634A (en) * 1988-12-02 1993-03-02 Lummus Crest Inc. Inhibition of coke formation during vaporization of heavy hydrocarbons
US4940828A (en) * 1989-10-13 1990-07-10 The M. W. Kellogg Company Steam cracking feed gas saturation
US5271827A (en) * 1990-11-29 1993-12-21 Stone & Webster Engineering Corp. Process for pyrolysis of hydrocarbons
US5364995A (en) * 1991-03-05 1994-11-15 Bp Chemicals Limited Polymer cracking
US5151158A (en) * 1991-07-16 1992-09-29 Stone & Webster Engineering Corporation Thermal cracking furnace
US5271809A (en) * 1991-08-28 1993-12-21 Selas-Kirchner Gmbh Pyrolytic furnace for the thermal cracking of hydrocarbons
US5389342A (en) * 1991-12-30 1995-02-14 Pillips Petroleum Company Apparatus for dehydrogenation process control
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5446229A (en) * 1992-12-18 1995-08-29 Amoco Corporation Thermal cracking process with reduced coking
US5372706A (en) * 1993-03-01 1994-12-13 Mobil Oil Corporation FCC regeneration process with low NOx CO boiler
US5358626A (en) * 1993-08-06 1994-10-25 Tetra International, Inc. Method for retarding corrosion and coke formation and deposition during pyrolytic hydrocarbon procssing
US6464858B1 (en) * 1994-08-25 2002-10-15 Phillips Petroleum Company Method for improving the yield of heavy hydrocarbons in a thermal cracking process
US5972206A (en) * 1994-12-26 1999-10-26 Institut Francais Du Petrole Flexible steam cracking process and corresponding steam cracking facility
US5981818A (en) * 1995-03-21 1999-11-09 Stone & Webster Engineering Corp. Integrated cracking and olefins derivative process utilizing dilute olefins
US6027635A (en) * 1995-12-27 2000-02-22 Institute Francais Du Petrole Continuous pyrolysis and decoking process for use in the production of acetylene
US6228253B1 (en) * 1997-06-05 2001-05-08 Zalman Gandman Method for removing and suppressing coke formation during pyrolysis
US6719953B2 (en) * 1997-06-10 2004-04-13 Exxonmobil Chemical Patents Inc. Process for the manufacture of olefins by a pyrolysis furnace with an internally finned U shaped radiant coil
US6312652B1 (en) * 1997-09-19 2001-11-06 Stone & Webster Engineering Corp. Ceramic dip pipe and tube reactor for ethylene production
US6013852A (en) * 1997-11-21 2000-01-11 Shell Oil Company Producing light olefins from a contaminated liquid hydrocarbon stream by means of thermal cracking
US5866745A (en) * 1998-01-26 1999-02-02 Abb Lummus Global Inc. Catalytic/oxidative promoted hydrocarbon pyrolysis
US6168709B1 (en) * 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US6632351B1 (en) * 2000-03-08 2003-10-14 Shell Oil Company Thermal cracking of crude oil and crude oil fractions containing pitch in an ethylene furnace
US6706246B2 (en) * 2001-02-26 2004-03-16 Abb Lummus Global Inc. System and method for the selective catalytic reduction of nitrogen oxide in a gas stream
US6685893B2 (en) * 2001-04-24 2004-02-03 Abb Lummus Global Inc. Pyrolysis heater
US6852294B2 (en) * 2001-06-01 2005-02-08 Conocophillips Company Alternate coke furnace tube arrangement
US6425757B1 (en) * 2001-06-13 2002-07-30 Abb Lummus Global Inc. Pyrolysis heater with paired burner zoned firing system
US20030070962A1 (en) * 2001-09-19 2003-04-17 Qingquan Zeng Pyrolysis furnace with new type radiant tubes arrangement and method of its operation and usage
US7090013B2 (en) * 2001-10-24 2006-08-15 Shell Oil Company In situ thermal processing of a hydrocarbon containing formation to produce heated fluids
US20030213687A1 (en) * 2002-04-10 2003-11-20 Platvoet Erwin M.J. Cracking furnace with more uniform heating
US20030209469A1 (en) * 2002-05-07 2003-11-13 Westlake Technology Corporation Cracking of hydrocarbons
US7138047B2 (en) * 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US6743961B2 (en) * 2002-08-26 2004-06-01 Equistar Chemicals, Lp Olefin production utilizing whole crude oil
US7019187B2 (en) * 2002-09-16 2006-03-28 Equistar Chemicals, Lp Olefin production utilizing whole crude oil and mild catalytic cracking
US20040147794A1 (en) * 2003-01-24 2004-07-29 Brown David J. Process for cracking hydrocarbons using improved furnace reactor tubes
US7125483B2 (en) * 2003-04-10 2006-10-24 Equistar Chemicals, Lp Corrosion control in olefin production plants
US6979757B2 (en) * 2003-07-10 2005-12-27 Equistar Chemicals, Lp Olefin production utilizing whole crude oil and mild controlled cavitation assisted cracking
US20050176831A1 (en) * 2004-01-09 2005-08-11 Taiji Inui Steam reforming system
US20050209495A1 (en) * 2004-03-22 2005-09-22 Mccoy James N Process for steam cracking heavy hydrocarbon feedstocks
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
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
US20060045828A1 (en) * 2004-09-01 2006-03-02 Aaron Timothy M Catalytic reactor

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102041031A (zh) * 2010-12-17 2011-05-04 惠生工程（中国）有限公司 乙烯裂解炉用穿膛柱结构及其制造方法
US20220119716A1 (en) * 2020-10-15 2022-04-21 Technip Process Technology, Inc. Hybrid ethylene cracking furnace
WO2022225691A1 (fr) * 2021-04-19 2022-10-27 Exxonmobil Chemical Patents Inc. Procédés et systèmes de vapocraquage de charges hydrocarbonées

Also Published As

Publication number Publication date
WO2009014949A1 (fr) 2009-01-29

Similar Documents

Publication Publication Date Title
JP5020640B2 (ja) 分解炉
EP1252254B1 (fr) Four de craquage multizone
EP0305799B1 (fr) Dispositif de chauffage pour pyrolyse
EP2310472B1 (fr) Procédé pour le décokage en marche productive d'un four pour le craquage d'une alimentation hydrocarbonée
US20230407186A1 (en) Electric furnace to produce olefins
US6852294B2 (en) Alternate coke furnace tube arrangement
EP2949728B1 (fr) Procédé d'opération d'un four de craquage d'éthylène
US20090022635A1 (en) High-performance cracker
EP1295930B1 (fr) Four de pyrolyse équipé d'un nouveau type d'arrangement de tubes radiants et son procédé de fonctionnement et usage
KR20140132013A (ko) 열 교환 장치 및 그 제조방법
CA3062425C (fr) Tube de transfert de chaleur pour traitement d'hydrocarbures
US20220154084A1 (en) Multi row radiant coil arrangement of a cracking heater for olefin production
EP4370630A1 (fr) Vapocraquage à chauffage électrique supplémentaire
MXPA06008885A (en) Cracking furnace

Legal Events

Date Code Title Description
AS Assignment

Owner name: SELAS FLUID PROCESSING CORPORATION, PENNSYLVANIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ZHAO, BAOZHONG;STANLEY, EDWARD F.;GARLAND, JOHN R.;AND OTHERS;REEL/FRAME:019600/0625;SIGNING DATES FROM 20070614 TO 20070719

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION