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EP0253633B1 - Four et procédé de craquage thermique - Google Patents

Four et procédé de craquage thermique Download PDF

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Publication number
EP0253633B1
EP0253633B1 EP19870306227 EP87306227A EP0253633B1 EP 0253633 B1 EP0253633 B1 EP 0253633B1 EP 19870306227 EP19870306227 EP 19870306227 EP 87306227 A EP87306227 A EP 87306227A EP 0253633 B1 EP0253633 B1 EP 0253633B1
Authority
EP
European Patent Office
Prior art keywords
flue gas
duct
furnace
tube
gas duct
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
Application number
EP19870306227
Other languages
German (de)
English (en)
Other versions
EP0253633A3 (en
EP0253633A2 (fr
Inventor
Peter Hubertus Kosters
Nico Jan Vossenberg
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.)
Dow Chemical Co
Original Assignee
Dow Chemical Co
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 Dow Chemical Co filed Critical Dow Chemical Co
Publication of EP0253633A2 publication Critical patent/EP0253633A2/fr
Publication of EP0253633A3 publication Critical patent/EP0253633A3/en
Application granted granted Critical
Publication of EP0253633B1 publication Critical patent/EP0253633B1/fr
Expired legal-status Critical Current

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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
    • C10G9/14—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

  • This invention relates to a hydrocarbon cracking furnace and to a hydrocarbon cracking method using said cracking furnace.
  • Thermal cracking of hydrocarbons is a technique which is practised widely in the hydrocarbon industry, and numerous configurations of thermal cracking furnaces have been proposed.
  • European Patent Specification No. 0074435 discloses a form of thermal cracking furnace in which a mixture of hydrocarbon and superheated steam is caused to flow through a reactor conduit, cocurrent with a flow of a heating gas surrounding the conduit.
  • thermal cracking reactor should be as short as possible, but should nevertheless provide for the maximum heat transfer over its length.
  • U.S.-A-4412975 discloses a form of thermal cracking reactor in which a tube containing the hydrocarbon to be cracked passes through a radiant enclosure, in which the tube is heated by radiation from the furnace walls.
  • This system like that disclosed in EP-B-0074435, suffers from the disadvantage that because the flue gases cool as they pass through the furnace, the temperature of the heat transfer surface of the heat exchanger varies along the length of the furnace. Thus, it is not possible to maintain the heat transfer surface at the optimum temperature for maximum heat transfer, along the whole of its length.
  • the factor which limits the heat transfer characteristics of a tubular cracking reactor will in general be the thermal failure temperature of the tubular reactor, which will generally be metallic.
  • the reactor tube is close to its thermal failure temperature in the region adjacent the burners, it will be at a temperature substantially lower than this at a point downstream of the burners.
  • U.S.-A-4412975 discloses various attempts to overcome this difficulty, by means of back-mixing of flue gases, and (in the discussion of prior art), the provision of multiple burners. Such attempts have met with only limited success, because a substantial temperature gradient along the length of the reactor still results, and the temperature of the existing flue gases is relatively high, leading to poor fuel economy.
  • a hydrocarbon cracking furnace (1) comprising at least one cracking reactor (8) having a first tube (14), connected to a feedstock inlet, said tube being open-ended downstream and being disposed substantially coaxially within a second tube (12), connected to an outlet for cracked products and closed proximate and around the open end of said first tube, said first and second tubes communicating at a first end (15) of the reactor, a burner (3) disposed proximate the said first end of the reactor, and orientated to generate a flow of hot flue gas in a flue gas duct (10) around the second tube, in a direction co-current with the flow of feedstock in an inner duct (11) defined by the annular space between the first and the second tubes, the said first end (15) of the reactor being disposed in the flow of flue gases from the burner (3), and the reactor extending downstream with respect to the flow of flue gases from the said first end.
  • This arrangement is particularly advantageous, because radiative heat transfer from the outer tube wall (i.e. the outer surface of the inner duct) to the inner tube wall takes place very readily through the fluid to be heated (e.g. the steam/hydrocarbon mixture).
  • the inner tube surface is heated to a temperature in excess of that of the surrounding fluid. Not only does this serve to pre-heat the incoming fluid in the inner tube, it also provides additional heating to fluid in the space between the inner and outer tubes by radiative transfer from the inner tube.
  • the internal surface of the outer of the two coaxial tubes which is responsible for heat exchange with fluid in the inner duct, can be maintained at a substantially constant temperature, along substantially the whole of its length, even though the temperature of the fluid within it is increasing, and the temperature of the surrounding flue gas is decreasing, by providing a continuous change in the heat exchange characteristics of the outer duct along its length as referred to above.
  • the outer wall of the inner duct which is generally a metallic tube, can be operated very close to its thermal failure temperature, along substantially the whole of its length, thus providing the maximum heat transfer.
  • the means defining the outer surface of the outer duct is preferably formed of a ceramic material (which term as used herein includes within its scope refractory materials of various kinds capable of withstanding the high temperature involved), since the temperature of operation of the outer duct will in general be substantially higher than that of the inner duct.
  • the cross section of the outer duct preferably varies along at least a portion of its length in such a manner as to provide in use an inwardly directed radiative heat flux from the said outer wall which varies along the said portion of the length of the outer duct, in such a way as to tend to compensate for fall in temperatures in fluid flowing in the outer duct.
  • the variation in cross-section of the outer duct may take the form of a variation (normally a decrease) in cross-sectional area of the duct, and/or an increase, preferably a continuous increase, in the surface area per unit length of the outer wall of the outer duct.
  • the construction is preferably such that, when flue gas from a burner at or adjacent an end of the inner duct is drawn through the outer duct, the heat transfer characteristics of the said outer wall of the outer duct are such as to cause the temperature of the surface of the outer wall of the inner duct over a portion of its length corresponding to the said portion of the outer duct to be substantially constant in use.
  • the said portion of the length of the duct over which the cross-section varies is preferably at least one quarter, more preferably at least one half, more preferably still at least three quarters, and most preferably substantially all of the length of the duct.
  • the change in cross section of the outer duct tends to compensate for the fall in temperature of the flue gases as they flow through the outer duct.
  • the temperature of the flue gases may fall along the duct in a typical embodiment from about 2000°C at the burner end to about 1500°C at the exhaust end.
  • the outer duct cross section as indicated, it is possible to maintain the outer wall temperature sufficiently high to provide the desired level of radiative heating to the inner duct.
  • the temperature of the outer duct wall in a cracking furnace in accordance with the invention may vary from 1600°C at the burner end to 1200°C at the exhaust end, preferably from 1500°C at the burner end to 1450°C at the exhaust end.
  • the particular temperature utilised will vary from installation to installation, depending not only on the geometry of the system, but also on the cracking reaction which it is desired to carry out.
  • the particular temperature profile utilised for the outer wall of the outer duct is preferably chosen so as to maintain the temperature of the wall of the inner duct which is in contact with the material to be cracked at at least 950°C, over a substantial part of its length.
  • the temperature of the inner wall of the outer duct is preferably as high as possible, typically greater than 1070°C, and as high as material limitations permit, over a substantial part of its length.
  • the surface area per unit length may be increased by providing on the inner surface of the outer duct a plurality of ribs, having a cross sectional area which increases continuously along the said portion of the outer duct.
  • the increase in surface area over the said region may preferably be continuous, for example by providing ribs having a cross sectional area which increases continuously, as described above,
  • the increase in surface area may, less preferably, be achieved by means of a number of small stepwise changes in the shape of the cross section of the outer duct, for example by constructing the outer duct from a plurality of blocks, joined along the length of the duct, each having a slightly increased internal area per unit length.
  • the cross sectional area of the outer duct preferably decreases over its length or preferably at least over the said portion of its length. This has the effect of increasing the velocity of the gas flow in the space between the inner and outer ducts, and thus increasing convective heat transfer between the gas and the wall of the outer duct.
  • the said decrease in cross sectional area may be achieved by providing the said ribs of increasing size as described above. Alternatively, or additionally, the decrease in cross sectional area may result from a stepwise or continuous decrease in diameter of the outer duct.
  • Raised ribs may be provided along the whole or part of the length of the outer wall of the outer duct, so as to provide the desired variation in surface area and in cross-section. Both the size and number of such ribs may be increased, over the length of the outer duct.
  • the outer surface of the duct is preferably formed by moulding a ceramic material, for example by moulding a ceramic material around a disposable former, having the desired number of ribs on the outer surface thereof.
  • the disposable former may be made of a foamed plastics material, for example polystyrene. After the ceramic has been allowed to set, the disposable former may be removed, by dissolution with a solvent, or, more preferably, simply by firing the ceramic to a temperature at which the plastics material is pyrolysed.
  • the ceramic casting is from 7.5 to 10 m in length. This method of construction results in low materials cost, and low fabrication costs, and can provide a structure which is substantially stronger with regard to thermal stresses, as compared with previous constructions.
  • a ceramic material may be cast by a compression moulding technique, for example using a metallic mould.
  • a compression moulding technique for example using a metallic mould.
  • the ceramic material is preferably provided with a plurality of elongate longitudinal grooves extending along the radiative surface thereof.
  • elongate grooves have been found to be of substantial benefit in maximising resistance of the ceramic material to thermal shock.
  • the elongate grooves may be for example about 1 cm in depth and 0.5 to 1 mm in width. They may conveniently be formed by drawing toothed comb-like members through the ceramic material before the material is fired.
  • the two coaxial tubes communicate at one end thereof, that end being located in the region of the heat exchanger occupied by the hottest flue gases.
  • the particular arrangement of the hydrocarbon cracking furnace in accordance with the invention is advantageous in providing optimum temperature distribution of the reactor tubes, without local "hot spots".
  • the cracking furnace of the invention may preferably, but not essentially, include a heat exchanger.
  • the thermal cracking furnace in accordance with the invention preferably includes a number of heat exchange tubes arranged in a parallel fashion.
  • Each such heat exchange tube may be provided within a generally hexagonal ceramic block, having a radiative surface area which varies continuously along a portion of its length.
  • Such hexagonal blocks fit conveniently together, and provide the greatest structural integrity, for minimum weight.
  • the heat exchangers may be provided in an array in which tubes are vertically staggered, to facilitate the supply of feedstock to the various heat exchange sections.
  • a thermal cracking furnace having a plurality of flue gas ducts in cast in a ceramic block, that a thermal cracking furnace can be produced which is readily adaptable to the cracking of alternative feedstocks.
  • Different feed stocks will, in general, require different thermal cracking temperatures, and heats of reaction.
  • the heat exchange temperatures of the inner duct through which the feed stock is passed can be controlled, by appropriate choice of the size and number of ribs formed on the ceramic material. Accordingly, different ceramic blocks, having different heat exchange characteristics, may be exchanged, within the same thermal cracking furnace, so as to accommodate different feedstocks.
  • thermal cracking furnace in accordance with the invention is such that an existing furnace may be very easily converted into a furnace in accordance with the invention, simply by providing a ceramic block and tube structure therein.
  • At least one additional heat exchanger is preferably incorporated to provide rapid cooling of the thermally cracked material, on its exit from the furnace area. Rapid cooling in this way minimizes the production of unwanted by-products.
  • the additional heat exchanger may be of the co-axial type described above, with high pressure water being supplied to the inner tube, whereby high pressure steam is generated in the outer tube.
  • a furnace for the thermal cracking of hydrocarbons comprises a casing 1, containing an inner layer 2 of an insulating material, which may for example be a ceramic material.
  • a burner 3 is located at one end of the casing 1, and is adapted to burn a suitable hydrocarbon feed material, supplied through line 4.
  • Combustion air for the burner 3 is supplied by a pump 7 through a conduit 6g and is pre-heated in heat exchangers 18a and 18b, and delivered to the vicinity of burner 3 via conduit 6b. Additional heating of this air can be achieved, if desired, by causing it to flow between casing 1 and insulating material 2 en route to burner 3.
  • the hydrocarbon fuel supplied by line 4 may if desired also be heated before passage to burner 3.
  • the furnace includes a block of eight heat exchangers, of which two are indicated generally at 8 in Figure 1 and which are illustrated in more detail in Figures 2 and 3.
  • Heat exchangers 8 comprises a ceramic block 9, having disposed therein a duct, again shown schematically at 10 in Figure 1, and in more detail in Figure 2 defined between block 9 and a tube 12, described in more detail below.
  • a large number of ducts for example six or eight will typically be utilised.
  • Figure 3 is a schematic view in the direction of arrows 3-3 in Figure 1, showing the construction of the outer duct of heat exchangers 8 from a plurality of generally hexagonal ceramic blocks 9 a to 9 h .
  • Blocks 9 a to 9 h in Figure 3 illustrate the progressive change in cross section of the hexagonal ceramic blocks along their length, as will be described in more detail hereinafter.
  • ducts 10 Disposed within ducts 10, are inner ducts 11, having three concentric tubes, an outer tube 12, the outer surface of which defines a heat exchange surface with flue gases produced by burner 3, an intermediate tube 13 for supplying the high temperature steam diluent, and an inner tube 14 for supplying feedstock.
  • ducts 10 are present in each of blocks 9 a to 9 h , but are illustrated only in block 9 a for clarity.
  • the various tubes 12, 13 and 14 meet at end 15 of tube 10.
  • Heat exchange tower 20 includes various heat exchangers, of conventional form, to preheat the hydrocarbon feed, for air preheat, and to preheat steam, for dilution of the hydrocarbon feed. Heat exchange tower 20 may also be used to preheat the fuel for burner 3, as described above.
  • heat exchange tower 20 includes heat exchangers 18 a and 18 b , for pre-heating the combustion air, as described above.
  • Tower 20 also includes heat exchangers 22 a , 22 b and 22 c for pre-heating the feed stock to be cracked, fed through line 23.
  • High temperature steam is supplied through line 25, via lines 25 a and 25 b to heat exchanger 26 a , and heat exchanger 26 b .
  • the high temperature steam produced in heat exchangers 26 a and 26 b is fed, together with the heated feedstock, to duct 11.
  • the feed stock is supplied by pipe 14, and super heated steam via pipe 13.
  • the naphtha feed stock is typically supplied to tube 14 at a temperature of approximately 620°C, and super heated steam to pipe 13 at a temperature of approximately 1100°C.
  • Heat exchange tower 20 also includes an additional heat exchange element 28, for preheating boiler feed water, for use in heat exchangers 17.
  • FIG. 2 illustrates an inner duct of the kind shown in Figure 1 in which the hydrocarbon to be cracked, for example naphtha, is supplied via conduit 30 to inner tube 14.
  • a relatively low amount of dilution steam is added to the hydrocarbon in the convection section.
  • the steam dilution ratios employed for the cracking of LPG, naphtha and gasoil are preferably (by weight) 0.3 to 0.6, 0.4 to 0.8, and 0.6 to 1.0 by weight respectively, more preferably about 0.4, 0.5 and 0.8 respectively.
  • Superheated steam is supplied via conduit 31 to the space defined between tubes 14 and 13.
  • Orifices may be provided along the length of tube 14, to enable the naphtha feedstock to mix with superheated steam supplied through conduit 31. Whilst contained within the tube 13, the hydrocarbon feed and superheated steam mixture is at a relatively low temperature, and insufficient for substantial thermal cracking to take place. At the end 15 of the duct 11, the hydrocarbon feed/steam mixture passes into the space defined by tube 13, and outer tube 12. Here, heat exchange takes place with the metallic surface of the outer tube 12. Because of the increasing surface area of the inner surface of blocks 9, the temperature of the outer surface of pipe 12 remains substantially constant over that portion of its length for which the radiative area per unit length increases.
  • the duct 10 in which the tube 12 is located is provided on its inner surface with inwardly projecting ribs as illustrated in more detail with reference to Figure 3.
  • Figure 3 is a schematic diagram, showing the change in the internal cross-section of the blocks 9 along their length.
  • Four general types of block are illustrated in Figure 3, and although at any given cross-sectional point along their length, all the ducts 10 will have the same cross-section, the various blocks 9 a to 9 h of Figure 3 illustrate the cross-section of blocks 9 at different points along their length.
  • blocks 9 c , 9 d , 9 g , and 9 h illustrate the cross-section employed for blocks 9 used at the end of the heat exchanger adjacent the burner 3.
  • the blocks 9 have a substantially constant cross-section, over a length of approximately 3 metres. Only 3 large support legs, 36, 37, and 38 are provided in the blocks 9, to support and locate tubes 12.
  • Additional ceramic blocks 41 are provided to support the shaped blocks 9 a to 9 h .
  • FIG. 1 Also illustrated in Figure 1 are various other lines, vessels, and heat exchangers, for example steam drum 45, and transfer line exchanger 46, of a kind conventionally employed in thermal cracking, the function of which need not be explained in detail.
  • steam drum 45 and transfer line exchanger 46, of a kind conventionally employed in thermal cracking, the function of which need not be explained in detail.
  • the thermal cracking furnace disclosed above has a number of substantial advantages as compared with conventional thermal cracking furnaces.
  • heat exchange tubes are placed within a large fireblock, and low residence times are achieved by using several small heat exchange tubes, rather than a single large one, so that the surface area to volume ratio increases.
  • the use of such heat exchangers, spaced throughout a fireblock makes is very difficult to obtain even distribution of heat over the pipe surfaces, particularly in view of their small size. This leads to coking rates which are different for the various heat exchangers, and consequently substantial pressure drops.
  • each heat exchanger has its own feedstock supply, and therefore the flow and pressure drop across each heat exchanger can be controlled independently.
  • hydrocarbon feedstock and superheated steam are supplied in a single inner lumen.
  • the particular design of the cracking furnace in accordance with the invention enables a substantially reduced overall furnace volume to be achieved for a given throughput.
  • a throughput which would require a furnace having a volume of 300 m3 with conventional designs can typically be achieved utilising a furnace in accordance with the invention having a volume of about 25 m3.

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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)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Claims (10)

  1. Un four (1) de craquage d'hydrocarbure, comprenant au moins un réacteur de craquage (8) comportant un premier tube (14), relié à une entrée de matière première, ledit tube ayant une extrémité aval ouverte et étant disposé de façon sensiblement coaxiale à l'intérieur d'un deuxième tube (12), relié à une sortie pour les produits de craquage et à proximité immédiate et autour de l'extrémité ouverte dudit premier tube, lesdits premier et deuxième tubes communiquant à une première extrémité (15) du réacteur, un brûleur (3) situé à proximité de ladite première extrémité du réacteur, et orienté de façon à générer un flux de gaz de fumée chaud dans un conduit de gaz de fumée (10) autour du deuxième tube, dans une direction de même sens que celle du flux de matière première dans un conduit interne (11) défini par l'espace annulaire compris entre le premier et le deuxième second tubes, ladite première extrémité (15) du réacteur étant placée dans le flux des gaz de fumée en provenant du brûleur (3), et le réacteur s'étendant en aval relativement à l'écoulement des gaz de fumée de ladite première extrémité.
  2. Un four conforme à la revendication 1, comportant un moyen (9) qui définit une paroi externe d'un conduit de gaz de fumée (10) pour contenir ledit écoulement du gaz de fumée chaud, ledit moyen (9) étant situé autour dudit conduit interne (11) pour permettre le transfert de chaleur entre ladite paroi externe et ledit conduit (11) dans lequel la surface de la section transversale du conduit de gaz de fumée (10) varie et/ou la surface par unité de longueur de la paroi externe du conduit de gaz de fumée (10) augmente sur au moins une partie de la longueur du conduit de gaz de fumée (10) pour permettre en cours d'utilisation un flux de chaleur par radiation dirigé vers l'intérieur à partir de ladite paroi externe qui varie le long de ladite partie de la longueur du conduit de gaz de fumée (10) de façon à compenser la chute de température du gaz de fumée qui s'écoule dans le conduit de gaz de fumée (10).
  3. Un four conforme à la revendication 2, dans lequel le moyen (9) définissant ladite paroi externe du conduit de gaz de fumée comporte une pluralité de nervures (30, 40) faisant saillie vers l'intérieur et ayant une surface en coupe transversale qui augmente le long de ladite portion de la longueur du conduit de gaz de fumée (10).
  4. Un four conforme à la revendication 3, dans lequel ladite surface en coupe transversale augmente continûment le long de ladite partie de la longueur du conduit de gaz de fumée (10).
  5. Un four conforme à l'une quelconque des revendications précédentes, dans lequel le tube (12) qui définit le conduit interne (11) consiste en une paire de tubes coaxiaux (12, 13), dans lequel le plus interne (13) des deux tubes coaxiaux est apte à fournir la matière première hydrocarbure à l'extrémité (15) du réacteur.
  6. Un four conforme à l'une quelconque des revendications 2 à 5, dans lequel ledit moyen (9) définissant la paroi externe du conduit de gaz de fumée consiste en un bloc de céramique.
  7. Un four conforme à l'une quelconque des revendications précédentes, dans lequel le tube (12) définissant le conduit interne consiste en un tube métallique.
  8. Un four conforme à l'une quelconque des revendications 2 à 7, dans lequel la surface en coupe transversale du conduit de gaz de fumée (10) diminue sur ladite portion de sa longueur en s'éloignant du brûleur (3).
  9. Un procédé de craquage d'hydrocarbure, qui consiste à envoyer une alimentation en hydrocarbure que l'on doit craquer à l'entrée de matière première (30) d'un four tel que défini dans l'une quelconque des revendications précédentes, et à générer à partir dudit brûleur un écoulement de gaz de fumée dans le conduit de gaz de fumée (10) pour chauffer et par là craquer la matière première hydrocarbure.
  10. Un procédé conforme à la revendication 9, dans lequel le four fonctionne de façon à maintenir la température du deuxième tube (12) sensiblement constante sur au moins une partie de sa longueur correspondant à ladite partie du conduit de gaz de fumée.
EP19870306227 1986-07-15 1987-07-14 Four et procédé de craquage thermique Expired EP0253633B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8617214 1986-07-15
GB868617214A GB8617214D0 (en) 1986-07-15 1986-07-15 Heat exchanger

Publications (3)

Publication Number Publication Date
EP0253633A2 EP0253633A2 (fr) 1988-01-20
EP0253633A3 EP0253633A3 (en) 1989-02-08
EP0253633B1 true EP0253633B1 (fr) 1992-12-02

Family

ID=10601076

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19870306227 Expired EP0253633B1 (fr) 1986-07-15 1987-07-14 Four et procédé de craquage thermique

Country Status (5)

Country Link
EP (1) EP0253633B1 (fr)
JP (1) JPS6338888A (fr)
DE (1) DE3782874T2 (fr)
ES (1) ES2036211T3 (fr)
GB (1) GB8617214D0 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101146893B (zh) * 2005-01-20 2013-01-02 特克尼普法国公司 将包含重质尾部馏分的烃进料裂化的工艺

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4418614C1 (de) * 1994-05-27 1996-02-08 Staudinger Gmbh Elektronik Ele Verfahren zum thermischen Behandeln von Kohlenwasserstoff-Verbindungen
DE4418597C1 (de) * 1994-05-27 1995-12-21 Staudinger Gmbh Elektronik Ele Reaktor zur Behandlung von Kohlenwasserstoff-Verbindungen
EP0890812A4 (fr) * 1996-03-29 2000-10-04 Mitsui Shipbuilding Eng Unite de chauffage de l'air a haute temperature et installations de traitement des dechets
US6675880B2 (en) 1996-03-29 2004-01-13 Mitsui Engineering And Shipbuilding Company Limited Air heater for recovering a heat of exhaust gas
MY134898A (en) 2002-01-25 2007-12-31 Sheel Internationale Res Mij B V Method for the preparation of lower olefines by steam cracking
CN101134160B (zh) * 2006-08-30 2010-06-30 中国石油天然气股份有限公司 一种催化裂解生产低碳烯烃的反应装置
EP3371137B1 (fr) * 2015-11-04 2021-08-04 ExxonMobil Chemical Patents Inc. Système et procédé de conversion avec tube chauffé

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1560891A (en) * 1923-12-27 1925-11-10 William L Ragwill Cracking still for mineral oils
US2721735A (en) * 1951-10-23 1955-10-25 Shell Dev Tubular heater with partial flue gas recirculation and heating method
US3910768A (en) * 1973-11-06 1975-10-07 Stone & Webster Eng Corp High pressure cracking furnace and system
US4412975A (en) * 1980-07-08 1983-11-01 Pullman Incorporated Fired process heater
DE3171796D1 (en) * 1981-05-19 1985-09-19 Exxon Research Engineering Co Supporting the weight of a structure in a hot environment
EP0074435B1 (fr) * 1981-09-08 1986-01-02 Dow Chemical (Nederland) B.V. Procédé et appareillage pour le craquage d'hydrocarbures, dispositif de mélange; appareillage et procédé pour la production de vapeur d'eau surchauffée; structure de bloc de radiation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101146893B (zh) * 2005-01-20 2013-01-02 特克尼普法国公司 将包含重质尾部馏分的烃进料裂化的工艺

Also Published As

Publication number Publication date
EP0253633A3 (en) 1989-02-08
GB8617214D0 (en) 1986-08-20
ES2036211T3 (es) 1993-05-16
DE3782874D1 (de) 1993-01-14
EP0253633A2 (fr) 1988-01-20
JPS6338888A (ja) 1988-02-19
DE3782874T2 (de) 1993-04-08

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