EP0305799B1 - Dispositif de chauffage pour pyrolyse - Google Patents

Dispositif de chauffage pour pyrolyse Download PDF

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Publication number
EP0305799B1
EP0305799B1 EP88113240A EP88113240A EP0305799B1 EP 0305799 B1 EP0305799 B1 EP 0305799B1 EP 88113240 A EP88113240 A EP 88113240A EP 88113240 A EP88113240 A EP 88113240A EP 0305799 B1 EP0305799 B1 EP 0305799B1
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EP
European Patent Office
Prior art keywords
pyrolysis
coil
heating surface
hydrocarbons
coils
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.)
Expired - Lifetime
Application number
EP88113240A
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German (de)
English (en)
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EP0305799A1 (fr
Inventor
Jorge Moises Fernandez-Baujin
John Vincent Albano
Andrei Rhoe
Kandasamy Meenakshi Sundaram
Charles Sumner
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CB&I Technology Inc
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ABB Lummus Crest Inc
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Publication of EP0305799A1 publication Critical patent/EP0305799A1/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/24—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
    • 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

Definitions

  • the production of light olefins (ethylene, propylene, butadiene and butylenes) and associated aromatics (benzene, toluene, ethylbenzene, xylenes and styrene) is usually carried out by the thermal cracking of hydrocarbon feedstocks in the presence of steam. This process is known as the steam pyrolysis of hydrocarbons for the production of olefins.
  • the hydrocarbon feedstocks used for the production of olefins range from essentially pure ethane to vacuum gas oils and any combination thereof. Hydrogen and methane are impurities found in the feed.
  • the process consists of a pyrolysis section and a recovery section.
  • the feedstock preheating system, the steam pyrolysis coils and the exchangers to cool the coil effluent are included in the pyrolysis section of the plant.
  • the majority of the feed preheating system and the pyrolysis coils are contained in the pyrolysis furnace or reactor. The chemical reactions of this process take place in the pyrolysis coils in the absence of catalyst.
  • the pyrolysis furnaces consist of a convection section and a radiant section or any combination thereof.
  • the hydrocarbon feed is first preheated in the convection section of the furnace.
  • Dilution steam is then added and the steam-hydrocarbon mixture is further preheated in the mixed preheat coil of the convection section.
  • the dilution steam is also preheated prior to addition to the hydrocarbon stream.
  • the mixture is preheated up to the required transition temperature for pyrolysis in the radiant section. This temperature is identified as the crossover temperature between the convection and the radiant sections. This temperature varies with the type of feedstock and with the specific coil design.
  • vaporization of the feed takes place in the mixed preheat coil and/or at the point where the dilution steam is injected.
  • the vaporization of the feedstock is external to the convection section coils to avoid potential coke laydown.
  • boiler feedwater, saturated steam and dilution steam may also be heated in the convection section. It should be noted that this description is only typical. The requirements for the heating services described above, as well as their locations and sizes in the convection section of a pyrolysis furnace, depend upon the specifications of each plant's requirements.
  • the pyrolysis coils where the hydrocarbon feed in the presence of dilution steam is pyrolyzed, are contained in the radiant section of the pyrolysis furnace or reactor.
  • the number of pyrolysis coils per radiant section is a function of the required ethylene capacity per pyrolysis furnace, the desired pyrolysis yields, the coil configuration and dimensions, the feedstock type and the terminal operating conditions such as coil outlet pressure. Transferline exchangers, followed by direct quenching with oil, are used to cool the effluent coming out from the coils.
  • the pyrolysis coils based on small diameter tubes have less capacity per coil than those based on large diameter tubes. Therefore, the number of pyrolysis coils with small diameter tubes required to meet the specified ethylene production per furnace is larger than the number required with coils of large diameter tubes.
  • the current practice in the design of pyrolysis coils includes three basic types.
  • One type employs small to moderate tube diameters of 0.4 to 1.6 cm (1 to 4 inches) with a single tube per pass and one or more passes per pyrolysis coil (1 to 8).
  • the second type employs large tube diameters of 1.6 to 2.75 cm (4 to 7 inches) also with a single tube per pass and several passes per coil (2 to 12).
  • the third type uses a combination of small and large tube diameters of 0.4 to 2.75 cm (1 to 7 inches) and multiple tubes per pass toward the front end of the coil and single tube per pass toward the back end of the pyrolysis coil, and several passes per coil (2 to 12).
  • the tube diameter could be constant throughout the coils or could be increasing from the first pass to the last pass of the pyrolysis coils.
  • the pyrolysis coils are located in a longitudinal plane in the radiant section of the pyrolysis furnaces.
  • the pyrolysis coils could be staggered or located in a single row or multiple rows.
  • the radiant heat source is provided by firing either burners from the lateral walls of the radiant section, or burners from the floor (hearth) of the radiant section or a combination thereof.
  • Pyrolysis coils with small diameter tubes although having better heat transfer characteristics, result in smaller capacity per coil when compared to the other two design types because of the faster coking rate observed during the cycle, and the increase in coil pressure drop due to the coke deposited on the coil inner walls during the run. This increase has a detrimental effect on the pyrolysis yield (decreasing olefins production and increasing fuel oil byproduct at constant feedstock conversion with cycle time) produced by the first design mentioned above.
  • the surface to volume ratio is also reduced along the direction of the flow in the pyrolysis coil.
  • the larger tube diameters in the second half of the pyrolysis coil reduce the coking rate and, thus, the effect of the deposited coke on the coil pressure drop and the concomitant detrimental effect on the pyrolysis yields.
  • the larger tubes ultimately result in a larger capacity coil.
  • the axial temperature profile of the reacting gases still approaches a straight line with a positive slope.
  • the drawback of the larger diameter tubes is the lower heat transfer coefficient resulting in higher metal temperatures.
  • the ultimate objective is to develop an axial gas temperature profile that maximizes the utilization of the metal surface available in the pyrolysis coil.
  • the target temperature profile is concave down and as close as possible to an isothermal profile instead of the almost straight line with positive slope or concave up profile achieved with the first two coil design types mentioned earlier.
  • the isothermal axial gas temperature profile represents the best heat utilization of the metal in the pyrolysis coil, i.e., for a given yield and run length, the maximum capacity per unit weight of pyrolysis coil metal and, thus, the least expensive pyrolysis coil.
  • One design approach is to use zone firing which requires the partitioning of the firebox into several compartments.
  • the firing system has to be properly controlled to achieve the zone firing effect.
  • the operating principle behind this design approach is to initiate the cycle with a straight line or a concave up temperature profile by firing uniformly throughout the pyrolysis coil or shifting the intensity of the firing more toward the outlet section of the pyrolysis coil. Gradually, during the progress of the run or as coking of the coil takes places, the firing is shifted from more intensity toward the outlet section of the coil to more intensity toward the inlet section of the coil.
  • an isothermal or concave down axial temperature profile is used to operate the coil.
  • the zone firing approach permits the utilization of higher capacity per coil at constant running time.
  • this approach has not been too widely practiced in the industrial production of ethylene.
  • the metal in the pyrolysis coil is fully utilized only when the temperature profile approaches isothermal conditions which, in this type of design, occurs only during a fraction of the running time.
  • the swage coil design approach has been utilized in a large number of worldwide ethylene plants since the seventies. Instead of using a firebox of complex construction and a very sophisticated and expensive firing control system, it relies on the coil configuration to achieve the concave down axial gas temperature profile during the entire running time. Because of this efficient utilization of the metal in the pyrolysis coil, the coil is characterized by larger production capacity at equal average yields and constant running time. The swage coil has a higher capacity and a lower coking rate resulting in a longer running time per cycle.
  • the coke formation in this inlet region is significantly less than in the second half of the coil.
  • the increases in metal temperature due to coke deposition on the walls are only moderate.
  • inserts located inside the outlet tubes are expected to act as nucleus for the growth of the coke formed during pyrolysis.
  • the utilization of inserts in this region would result in shorter than desirable run lengths, higher than desirable pressure drops, poor operating reproducibility of conditions and significant losses in olefins yields.
  • the present invention relates to the incorporation of extended surfaces on the inlet portion of a pyrolysis coil in order to make the axial gas temperature profile even closer to an isothermal profile than it has been possible to achieve with uniform firing in the pyrolysis coils currently used in the olefins production industry.
  • This permits higher production capacity per unit weight of pyrolysis coil while preserving the desired pyrolysis yields and on-stream time in between decoking cycles.
  • this invention at constant ethylene production per pyrolysis coil, permits longer on-stream time and/or somewhat higher ethylene yields. More specifically, the invention involves the placing of the extended surface in the first half and preferably the first quarter of the coil and preferably involves the use of studs or longitudinal straight fins or ribs on either the outside or the inside of the tubes or both locations.
  • a vertical tube type pyrolysis heater supported on structural steel framework generally indicated as 10.
  • the heater is comprised of outer walls 11 and 12, inner walls 13 and 14, end walls 15 and floors 16 and 17.
  • the outer walls 11 and 12 are substantially parallel to inner walls 13 and 14 with the height of outer walls 11 and 12 extending above the height of inner walls 13 and 14.
  • Mounted in outer walls 11 and 12 and inner walls 13 and 14 are a plurality of vertical rows of high intensity radiant type burners, generally indicated at 18.
  • the floors 16 and 17 extend between the outer walls 11 and 12 and inner walls 13 and 14, respectively.
  • the floors 16 and 17 are provided with floor burners, generally indicated as 19 which are preferably of the flame type.
  • End walls 15 are in the shape of an inverted U thereby forming an open area 22 permitting access to the burners 18 mounted in the inner walls 13 and 14.
  • inner roof 25 Horizontally positioned and mounted on inner walls 13 and 14 is inner roof 25.
  • upper roof 26 mounted on outer wall 11 and end walls 15.
  • upper roof 27 is horizontally positioned and extends inwardly from outer wall 12 and is mounted on outer wall 12 and end walls 15.
  • Mounted on upper roofs 26 and 27 are upper walls 28 and 29 which form with the upper extending portions of end walls 15, a convection zone generally indicated as 30. All of the walls, floors and roofs are provided with suitable refractory material.
  • process coils 31 and 32 suitably mounted from supporting structure 10 by hangers 33.
  • the process coils 31 and 32 are positioned intermediate the outer and inner walls 11 and 13 and 12 and 14, respectively. The configuration of these process coils will be described in more detail hereinafter.
  • Mounted within the convection zone 30 are horizontally disposed conduits, schematically illustrated and generally indicated as 35.
  • the conduits 35 are in fluid communication with the process coils 31 and 32 through crossovers 36.
  • a second section of horizontally disposed conduits generally indicated as 38.
  • Inlet and outlet manifolds 38A and 38B are in fluid communication with the conduits 38.
  • the burners 18 are supplied with the fuel through lines 40 from a plurality of manifolds 39.
  • the fuel is introduced into manifolds 39 through a manifold 41 under control of valves 42.
  • the flow of fuel to burners 18 may be varied in vertical rows depending on the described severity of firing of the process coils 31 and 32.
  • Individual burners may be further adjusted by valves 44 in lines 40 with the total flow of fuel to the heater being controlled by valve 45. It is understood that the burners mounted in outer walls 11 and 12 and inner walls 13 and 14 have similar manifold means which is not shown.
  • lines 46 carry the fuel to the floor burners.
  • FIG. 2 there is schematically illustrated a layout of the process coil 31 and it is to be understood that the process coil 32 would be similar.
  • This general type of pyrolysis heater is described in U.S. Patent 3,274,978.
  • the present invention is also applicable to pyrolysis coils that can be installed in other types of heaters currently used in industry.
  • Process coil 31 is generally of the swage type previously discussed and consists of a first pass 46, a second pass 47, a third pass 48, a fourth pass 49, a fifth pass 50 and a sixth pass 51.
  • the first pass 46 comprises four tubes
  • the second pass 47 and the third pass 48 each comprise two tubes
  • the passes 49, 50 and 51 each comprise one tube.
  • this coil should be considered typical only and not limiting the present invention.
  • the present invention is applicable to pyrolysis coils of any configuration and tube dimensions.
  • extended heating surface 52 is located on the four tubes of first pass 46.
  • This extended heating surface can be in the form of studs or straight longitudinal fins or ribs.
  • the studs may be of any desired shape but they are preferably cylindrical.
  • the size and number of studs or fins per unit length of pyrolysis tubing are selected according to the process parameters of any particular installation.
  • the studs may be 0.2 cm (0.5 inches) in diameter with a length ranging from 0.2 to 0.3 cm (0.5 to 0.75 inches). There may be 8 to 12 studs around the circumference of the tube at any one plane.
  • Figure 3 illustrates a short section of tube with studs. Studs are applicable to the outside of the tubes.
  • the fins may be 0.5 cm (0.2 inches) in height having 6 to 10 fins around the circumference of the tubes.
  • Figure 4 illustrates a cross-section of a tube with straight longitudinal fins or ribs around the inside circumference thereof.
  • the extended heating surface is installed in the first half of the pyrolysis coil and preferably in the first quarter. As indicated, the embodiment illustrated in Figure 2 has the studs only in the first pass.
  • the coil configuration is four tubes in the first pass, two tubes in each of the second and third passes, and one tube in each of the fourth, fifth and sixth passes:
  • an isothermal gas temperature profile would be desired.
  • the use of zone firing and the prior art swage coil design both bring the temperature profile closer to the isothermal.
  • the use of the internal and/or external extended heating surface of the present invention in the first half or quarter of the coil brings the temperature profile even closer to the isothermal.
  • Use of extended heating surface in the last part of the coil would tend to take the temperature profile further away from a isothermal profile as well as create the coking previously mentioned.
  • the use of the extended surface in the first part of the coil maintains or enhances the run length or cycle time, maintains or enhances pyrolysis selectively toward olefins and enhances ethylene capacity per unit weight of tube metal and any combination thereof.

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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)
  • Processing Of Solid Wastes (AREA)

Claims (7)

  1. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures, comprenant:
    a) une chambre chauffante radiante,
    b) au moins un serpentin de traitement tubulaire comportant une première moitié et une seconde moitié pour le traitement du fluide dans ladite chambre chauffante,
    c) une pluralité de brûleurs radiants pour chauffer ledit au moins un serpentin de traitement tubulaire, et
    d) ledit au moins un serpentin de traitement tubulaire comprenant, à l'intérieur d'au moins une portion de sa première moitié uniquement, une surface chauffante agrandie posée sur et saillant de la surface interne et/ou externe dudit serpentin de traitement tubulaire, ladite surface chauffante agrandie augmentant ainsi l'absorption de chaleur radiante.
  2. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 1, dans lequel ladite surface chauffante agrandie comprend une surface chauffante posée sur et saillant extérieurement de la surface externe dudit serpentin de traitement tubulaire.
  3. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 2, dans lequel ladite surface chauffante agrandie comprend des plots.
  4. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 1, dans lequel ladite surface chauffante agrandie comprend une surface chauffante s'étendant longitudinalement posée sur et saillant intérieurement de la surface interne dudit serpentin de traitement tubulaire.
  5. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 4, dans lequel ladite surface chauffante agrandie comprend des ailettes ou nervures longitudinales rectilignes.
  6. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 1, dans lequel ladite surface chauffante agrandie est située uniquement dans le premier quart dudit serpentin de traitement.
  7. Réchauffeur de pyrolyse pour la pyrolyse des hydrocarbures suivant la revendication 1, dans lequel ladite surface chauffante agrandie est située uniquement dans ladite première passe dudit serpentin de traitement tubulaire.
EP88113240A 1987-09-01 1988-08-16 Dispositif de chauffage pour pyrolyse Expired - Lifetime EP0305799B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US9180987A 1987-09-01 1987-09-01
US91809 1987-09-01

Publications (2)

Publication Number Publication Date
EP0305799A1 EP0305799A1 (fr) 1989-03-08
EP0305799B1 true EP0305799B1 (fr) 1991-10-23

Family

ID=22229753

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88113240A Expired - Lifetime EP0305799B1 (fr) 1987-09-01 1988-08-16 Dispositif de chauffage pour pyrolyse

Country Status (9)

Country Link
EP (1) EP0305799B1 (fr)
JP (2) JPS6470590A (fr)
KR (1) KR900005091B1 (fr)
CN (1) CN1015469B (fr)
BR (1) BR8804460A (fr)
CA (1) CA1309841C (fr)
DE (1) DE3865785D1 (fr)
ES (1) ES2028211T3 (fr)
IN (1) IN170778B (fr)

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0519230A1 (fr) * 1991-06-17 1992-12-23 Abb Lummus Crest Inc. Dispositif de chauffage pour pyrolyse
US5151158A (en) * 1991-07-16 1992-09-29 Stone & Webster Engineering Corporation Thermal cracking furnace
FR2688797A1 (fr) * 1992-03-20 1993-09-24 Procedes Petroliers Petrochim Four de vapocraquage d'hydrocarbures a faisceau de tubes.
GB2314853A (en) * 1996-07-05 1998-01-14 Ici Plc Reformer comprising finned reactant tubes
US6419885B1 (en) 1997-06-10 2002-07-16 Exxonmobil Chemical Patents, Inc. Pyrolysis furnace with an internally finned U shaped radiant coil
FR2768153A1 (fr) * 1997-09-09 1999-03-12 Procedes Petroliers Petrochim Four tubulaire de vapocraquage d'hydrocarbures a rendement et capacite elevee
US6685893B2 (en) * 2001-04-24 2004-02-03 Abb Lummus Global Inc. Pyrolysis heater
US6644358B2 (en) 2001-07-27 2003-11-11 Manoir Industries, Inc. Centrifugally-cast tube and related method and apparatus for making same
US7004085B2 (en) * 2002-04-10 2006-02-28 Abb Lummus Global Inc. Cracking furnace with more uniform heating
US20030209469A1 (en) * 2002-05-07 2003-11-13 Westlake Technology Corporation Cracking of hydrocarbons
GB0420971D0 (en) 2004-09-21 2004-10-20 Imp College Innovations Ltd Piping
US7749462B2 (en) 2004-09-21 2010-07-06 Technip France S.A.S. Piping
US8029749B2 (en) 2004-09-21 2011-10-04 Technip France S.A.S. Cracking furnace
GB0817219D0 (en) 2008-09-19 2008-10-29 Heliswirl Petrochemicals Ltd Cracking furnace
CA2738273C (fr) * 2011-04-28 2018-01-23 Nova Chemicals Corporation Bobine de chaudiere avec protuberances sur sa surface exterieure
BR112014002075B1 (pt) 2011-07-28 2019-05-28 Sinopec Engineering Incorporation Forno de craqueamento de etileno
CA2818870C (fr) 2013-06-20 2020-10-27 Nova Chemicals Corporation Tubes de chaudiere a tiges
CA2843361C (fr) 2014-02-21 2021-03-30 Nova Chemicals Corporation Tubes de chaudiere a tiges
CN106197021B (zh) * 2015-05-06 2018-12-25 中国石油天然气股份有限公司 管式加热炉管内介质流型调节装置
CN111606025B (zh) * 2020-04-22 2021-09-07 广东生波尔光电技术有限公司 特种工件镀膜设备
CN115307145B (zh) * 2022-07-26 2024-08-30 昆明理工大学 一种热解气化燃烧一体式余热循环利用装置

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3274978A (en) * 1964-02-24 1966-09-27 Lummus Co Vertical tube fluid heater
US4342642A (en) * 1978-05-30 1982-08-03 The Lummus Company Steam pyrolysis of hydrocarbons
GB2021632B (en) * 1978-05-30 1982-10-20 Lummus Co Pyrolysis of hydrocarbons
JPS60179405A (ja) * 1984-02-24 1985-09-13 Mitsui Toatsu Chem Inc 共粉砕方法

Also Published As

Publication number Publication date
EP0305799A1 (fr) 1989-03-08
KR900005091B1 (ko) 1990-07-19
IN170778B (fr) 1992-05-16
KR890005245A (ko) 1989-05-13
JPH0659447U (ja) 1994-08-19
CN1015469B (zh) 1992-02-12
JPS6470590A (fr) 1989-03-16
BR8804460A (pt) 1989-03-28
CN1033284A (zh) 1989-06-07
DE3865785D1 (de) 1991-11-28
ES2028211T3 (es) 1992-07-01
CA1309841C (fr) 1992-11-10

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