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EP0419643B1 - Verfahren und apparat zur entkoksung von dampfkrackanlagen - Google Patents

Verfahren und apparat zur entkoksung von dampfkrackanlagen Download PDF

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Publication number
EP0419643B1
EP0419643B1 EP90907094A EP90907094A EP0419643B1 EP 0419643 B1 EP0419643 B1 EP 0419643B1 EP 90907094 A EP90907094 A EP 90907094A EP 90907094 A EP90907094 A EP 90907094A EP 0419643 B1 EP0419643 B1 EP 0419643B1
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EP
European Patent Office
Prior art keywords
installation
particles
gas
solid particles
steam
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
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EP90907094A
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English (en)
French (fr)
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EP0419643A1 (de
Inventor
Eric Lenglet
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Procedes Petroliers et Petrochimiques
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Procedes Petroliers et Petrochimiques
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Filing date
Publication date
Priority claimed from FR8904986A external-priority patent/FR2645873B1/fr
Priority claimed from FR8909373A external-priority patent/FR2649717B1/fr
Priority claimed from FR8909375A external-priority patent/FR2649761B1/fr
Priority claimed from FR8913070A external-priority patent/FR2652817B1/fr
Priority claimed from FR8914118A external-priority patent/FR2653779B1/fr
Application filed by Procedes Petroliers et Petrochimiques filed Critical Procedes Petroliers et Petrochimiques
Publication of EP0419643A1 publication Critical patent/EP0419643A1/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C10G9/16—Preventing or removing incrustation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
    • F28G1/00—Non-rotary, e.g. reciprocated, appliances
    • F28G1/12—Fluid-propelled scrapers, bullets, or like solid bodies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00—Chemistry of hydrocarbon compounds
    • Y10S585/949—Miscellaneous considerations
    • Y10S585/95—Prevention or removal of corrosion or solid deposits

Definitions

  • the invention relates to a method of decoking an installation for steam cracking of hydrocarbons, as well as steam cracking installations comprising the means for implementing this process.
  • a first method consists in circulating a stream of neutral gas carrying metal particles of relatively large dimensions (250 -2500 ⁇ m) in an oven connected to the atmosphere.
  • Another method proposes carrying out continuous sanding of the steam cracking installation, by injecting sand into the liquid hydrocarbon charge.
  • the sand particles standard sand with an average diameter of 200-1000 ⁇ m
  • the subject of the invention is a method of decoking an installation for steam cracking of hydrocarbons, which does not have the drawbacks of known methods.
  • It also relates to a process of this type, making it possible to decoke the furnace and possibly the indirect quenching boiler of the installation, without it being necessary to stop the operation of the installation, without risking deteriorate the installation itself and without pollution by solid particles from the parts of the installation which are located downstream.
  • the invention proposes a method for decoking an installation for steam cracking of hydrocarbons, consisting in eliminating by erosion at least part of the coke deposited on the internal walls of the installation, in particular in the steam cracking oven and the indirect quenching boiler, by means of solid particles conveyed by a current of vector gas at high speed, characterized in that the decoking is carried out during the operation of the installation, the vector gas being constituted at least in part by the charge hydro-carbides and water vapor which contains solid particles having an average diameter of less than approximately 150 ⁇ m, with a very low solid / gas ratio, so that the gas-solid particle mixture behaves like a gas with a slight erosion capacity.
  • the process according to the invention therefore makes it possible, not to fracture by violent impacts of massive solid particles, the layer of coke deposited on the internal walls of the installation, but to erode it gently and regularly without risk for the walls of the installation.
  • This process allows simultaneous decoking of the steam cracking furnace and that of the indirect quenching boiler: for example, the quantity of solid particles conveyed by the gas stream at the inlet of the indirect quenching boiler can be increased, to compensate the decrease in the flow speed of this gas stream in this boiler. It is also possible to decoke the convection zone, in particular at the dry point, by sequentially injecting the aforementioned particles, supplied with the dilution vapor.
  • decoking is understood to mean the effective removal of at least part of the coke which is deposited on the walls (reduction or elimination of a layer of coke already formed, cancellation or reduction of the rate of formation of a layer of coke).
  • the gas-solid particle mixture is cooled at the outlet from the steam cracking oven to an intermediate temperature below about 600 ° C., determined to avoid any condensation of liquid, then at least separated most of the solid particles of the carrier gas in at least one cyclone, the pressure level is increased by at least a portion of the solid particles separated from the carrier gas in the cyclone, and they are recycled in the steam cracking installation.
  • the cyclone for separating solid particles can be made of low-alloy steel, therefore inexpensive, since it is not subjected to very high temperatures. Direct quenching by injection of liquid to which the carrier gas is subjected at the outlet of the cyclone makes it possible to trap the residual solid particles. The cracked gases are thus completely purified before the compression zone.
  • the solid particles used preferably have an average diameter of between 5 and 100 ⁇ m, approximately and the solid / gas ratio is less than 10% by weight, being preferably between 0.01% and 10%, and generally between 0 , 1 and 8% by weight.
  • the quantities of particles are small enough so that the particles hardly ever meet (no shocks); the mixture is therefore not comparable to a fluidized or entrained bed, but to a gas.
  • the very fine particles are mainly distributed throughout the volume of the gas, due to the predominant turbulence forces. We therefore obtain a gas seeded with fine particles, distributed throughout the volume, capable of a slight erosion action thanks to multiple low energy impacts, acting by running in and not by massive fracturing of coke (flaking).
  • the velocities of the particles in the oven are between 70 and 480 m / s (in general between 130 and 480 m / s, more particularly between 130 and 300 m / s). In the quenching boiler, they are 40 to 150 m / s.
  • the most suitable amounts of particles depend on the nature of the particles, the rate of coke deposition (linked to the nature of the charge), and the local conditions of speed and turbulence.
  • the average size of the solid particles is between 4 or 5 and 85 ⁇ m, and the solid / gas ratio is between 0.1 and 8% by weight, for example between 0.1 and 3% by weight
  • the solid particles brought into the installation can be injected at several points thereof, for example in one or more parts of the steam cracking furnace and at the inlet of the indirect quench boiler.
  • the solid particles separated from the carrier gas in the cyclone are mixed with water or with a hydrocarbon-based liquid substantially free of heavy aromatic pyrolysis compounds, such as for example only a fraction of the charge of hydrocarbons to be cracked, and the solid particles-liquid mixture is recycled by pumping in the installation.
  • the flow rate and the temperature of the particle-liquid mixture can be determined in order to obtain an almost instantaneous vaporization of the liquid upon injection of the mixture into the steam cracking installation.
  • a continuous flow of liquid is produced from a source line, to form a wetted wall situated around and below the zone of arrival of the solid particles.
  • the particles leaving the cyclone are collected in a balloon, this balloon is isolated, it is pressurized by means of a stream of superheated steam, and at least part of the particles are recycled in the installation using this stream of water vapor.
  • the solid particles used in the process according to the invention can advantageously be substantially spherical inorganic or metallic particles formed by gas atomization, such as porous particles based on silica or alumina, and can consist, for example, of particles catalytic cracking catalysts (zeolites), already used (having an average diameter of 60 - 80 ⁇ m) These solid particles can also consist of a mixture of two types of particles, some being metallic coke catalyst particles, which are relatively soft under the conditions of steam cracking, the others being harder and more erosive. Other particles (particles of coke, ground coal, cement, ores, pig iron, steel, carbides, stellites, angular particles ...) can also be used under the conditions of the erosive gas according to the 'invention.
  • the relatively soft coke catalyst metal particles are likely to leave marks on a exposed metal part of a wall internal of the installation, to form by their catalytic action on this part a protective layer of coke which will cover this part and protect it from too intense erosion.
  • the process can also consist in allowing a layer of coke to form on the internal walls of the steam cracking oven, and then maintaining the thickness of this coke layer at around a predetermined average value, by erosion by the aforementioned solid particles.
  • This coke layer is in fact a layer of progressive thickness along the cracking tube, and its thickness is maintained after its formation at an average value (corresponding to a coking state of the predetermined tube).
  • This relatively thin layer of coke (between 0.5 and 4 mm approximately, preferably between 1 and 3 mm) protects the internal walls of the installation from erosion, all the more since this layer rapidly becomes very hard and very difficult to fracture or erode due to the progressive calcination of the coke which occurs during the stay at high temperature (around 1000 ° C. in the wall).
  • its thickness is maintained at a substantially constant value, by continuous or substantially continuous erosion of the coke, as it is deposited on this protective layer.
  • the conditions for controlling erosion by solid particles are less critical, and we can admit a greater tolerance on the sizes of solid particles, their nature, and their distribution in the carrier gas.
  • the process does not necessarily, in the strict sense, decoking, but elimination of the newly formed coke, more fragile, as it is formed, to obtain a substantially stationary coking state, or a very coking speed. low.
  • the injection of particles can be continuous, or discontinuous, preferably at close intervals.
  • the invention also proposes an installation for steam cracking of hydrocarbons, containing a steam cracking oven with tubes for circulation of a load of hydrocarbons, a boiler for indirect quenching of the gaseous effluents leaving the oven, and means for direct quenching by injection.
  • the installation further comprising means, such as a cyclone, for separating solid particles and gas, which are provided at the outlet of the indirect quenching boiler.
  • this installation also comprises means for recycling the solid particles separated from the gas, as well as means for making up solid particles.
  • means for recycling the solid particles separated from the gas we can thus compensate for the quantity of particles consumed in the separation means, which can have a very high efficiency, for example of the order of 95 to 99%, but nevertheless less than 100%.
  • the installation also includes means for withdrawing used particles.
  • the installation comprises a storage tank for solid particles, the inlet of which is connected to the outlet of the solids of the above-mentioned separation means, and the outlet of which is connected to a conduit injection of particles into the installation, means for isolating this tank, such as valves, and means for connecting this tank to a source of pressurized gas making it possible to increase the internal pressure of the tank to a value at least equal to that of a particle injection point in the installation.
  • the solid particles are transported to the injection points either by gravity flow or in the form of a solid-gas suspension in dilute phase, without the need to use a vector gas stream at very high speed, which also reduces pipe erosion.
  • the installation comprises a second tank mounted between the outlet of the separation means and the inlet of the first tank mentioned, as well as means for isolating this second tank, such as valves, and means for retaining the large particles, provided inside the second tank.
  • This second tank can also be installed in parallel with the first tank.
  • the second tank collects the solid particles recovered at the outlet of the separation means, during the emptying of the first tank mentioned.
  • the source of pressurized gas is connected to the pipe for injecting particles into the installation. It is then the current of carrier gas used for injecting the particles into the installation which also serves to increase the pressure in the tank. This avoids, due to the balancing of the tank pressure by the carrier gas, an overpressure capable of compacting the solid particles.
  • the carrier gas is for example a fraction of the charge or of the superheated steam.
  • the means for recycling the solid particles comprise means for injecting a flow of gas devoid of heavy aromatics in the lower part of the separation means, to form with the solid particles recovered a gas-solid suspension at the outlet. of these means, and an ejector-compressor connected to the outlet of the aforementioned separation means and supplied with a flow of auxiliary gas at high pressure, to recompress the gas-solid suspension towards its point of injection into the installation.
  • This ejector should preferably be made of an erosion-resistant material (cast iron or ceramic material).
  • the invention provides means for injecting solid particles into the hydrocarbon charge vaporized upstream or at the inlet. of the manifold, means producing turbulent flow in the manifold at a speed sufficient to substantially avoid any deposit of solid particles in the manifold, supply nozzles mounted at the end of the tubes and extending inside the manifold , each nozzle comprising an inlet section which is oriented towards the upstream end of the collector and which has a component in a plane perpendicular to the mean direction of flow in the collector; advantageously, means are also provided for capturing solid particles at the downstream end of the collector.
  • the turbulence of the flow in the collector a correct homogeneity of the gas-particle mixture is obtained throughout the collector.
  • the ends which are provided at the ends of the tubes in the collector make it possible to supply these tubes in a regular and substantially constant manner with particles, whatever the place of the tubes in the collector.
  • the inlet section in the end pieces which has a front component facing the flow makes it possible avoid too pronounced changes of direction when entering the tubes, which would cause gas-particle separation phenomena and lead to an irregular distribution of the particles.
  • These tips also constitute very efficient turbulence generators in the collector.
  • the means for capturing an excess of particles which are provided at the downstream end of the collector make it possible to avoid over-supply of the last tube of the collector, or an obstruction of the latter by an excess of particles.
  • These means may for example be a filter, a settling chamber, a cyclone, or equivalent means making it possible to remove an excess of particles, and in particular the most massive particles.
  • These means can advantageously be placed in the region of the downstream end of the collector comprising for example the last two tubes, so as to collect relatively massive particles, progressing along the lower generatrix of the collector, so that these particles do not feed not the last tube with an excess of solids which would lead to an erosive capacity very different from the average value.
  • the installation comprises, at the downstream end of the manifold, means for withdrawing a fraction of the gas-solid particle flow rate flowing in the manifold, and recycling means, upstream or at the inlet of the manifold, of the fraction taken from the gas-solid particle flow.
  • the collector then behaves like a collector of infinite length, not comprising a "last" tube fed by the residual fraction of the gas-particle mixture.
  • a section restriction such as a neck or a venturi or a tube of smaller diameter, is advantageously provided at the entrance of each tube, in downstream of the aforementioned nozzle.
  • This section restriction makes it possible to regularize and standardize the gas flow rates circulating in the various tubes.
  • the installation can advantageously include means for measuring the pressure drop in the tubes of the steam cracking furnace, means for measuring the flow rate of the load of hydrocarbons to be cracked or the dilution water vapor, means for correcting the pressure drop as a function of this measured flow rate, and means for regulating the pressure loss corrected by controlling the flow rate of solid particles recycled in the installation.
  • the reference I denotes the curve of variation of the efficiency of the separation of a cyclone as a function of the size of the solid particles brought to this cyclone.
  • Reference II designates the curve of variation of the erosion capacity of solid particles as a function of their size.
  • the separation efficiency of a cyclone tends asymptotically to 100% when the size of the solid particles becomes greater than a value d1 for which the separation efficiency is for example 99%.
  • the erosion capacity of solid particles having this dimension is relatively low, and the rest for a range of dimensions around d1.
  • the separation efficiency of the cyclone decreases sharply, while the erosion capacity of these particles becomes substantially zero. Conversely, when the particle size is much greater than d1, the separation efficiency of the cyclone is almost equal to 100%, and the erosion capacity of the particles is very large and similar to the action of sandblasting, l 'erosion being violent and irregular.
  • the invention provides for choosing a range d1, d2 of particle size for which the cyclone separation efficiency will be greater than a determined value, for example 95 or 99%, and the erosion produced by these particles will be light and regular. .
  • FIG. 2 A steam cracking installation according to the invention has been shown diagrammatically in FIG. 2.
  • This installation comprises a furnace 10 with 12 single-pass tubes 12 supplied with hydrocarbons at one of their ends by a reader neck 14 and comprising at their opposite end, at the outlet of the oven, individual quenching boilers 16 connected to an outlet manifold 18.
  • the hydrocarbon charge to be vaporized is brought to the liquid state by a line 20 in a convection zone 22 of the furnace allowing its heating and its vaporization.
  • a pipe 24 for supplying water vapor joins the pipe 20 in this zone 22 of the furnace 10.
  • a preheating pipe 26 makes it possible to bring the mixture of vaporized hydrocarbons and water vapor to the supply manifold 14 steam cracking tubes 12.
  • the outlet manifold 18 is connected to a cyclone 28, or to several cyclones mounted in series and / or in parallel, comprising an upper pipe 30 for the outlet of the gaseous effluents and a lower pipe 32 for the outlet of the solid particles.
  • the lower conduit 32 opens into a reservoir 34, the bottom of which is filled with a liquid 36, which may be water or preferably a light hydrocarbon liquid substantially free of heavy aromatic pyrolysis compounds.
  • the base of the reservoir 34 is connected by a pump 38 to means for injecting the mixture of solid particles and liquid at various points in the installation, in particular at the inlet of the pipe 26 or in the supply manifold 14. may also provide injection points between the outlet of the furnace 10 and the inlet of the indirect quenching boilers 16.
  • the injections are made with atomization by steam, or self-vaporization by "flash" expansion.
  • the suspension must be reheated before injection, by means not shown.
  • the atomization and liquid flow conditions are calculated to allow complete vaporization of the atomized suspension, upon injection (instant vaporization, to avoid particle sticking).
  • Part of the liquid-solid particle mixture is brought, as shown diagrammatically at 40, to the upper part of the reservoir 34, so that the liquid can form a continuous film covering the entire internal wall of the reservoir 34 and trapping the solid particles in the as they exit the conduit 32.
  • the liquid flows in continuous motion from a "source line" on the wall of the reservoir 34, without making droplets.
  • the liquid 40 is driven by a vortex movement to increase the effect of washing and entrainment of particles on the wet wall of the reservoir 34.
  • the liquid supplied at 40 is advantageously decanted liquid, substantially free of particles, withdrawn in the reservoir 34 by a specific pump not shown.
  • the hydrocarbon liquid used in the tank 34 can be a fraction of the load of hydrocarbons to be cracked, which is brought into the lower part of the tank by a line 42.
  • Recycled pyrolysis gasoline can optionally be added to this fraction of the hydrocarbon charge, as shown diagrammatically at 44, or else may constitute the liquid 36 itself.
  • solid particles possibly in the form of a solid-hydrocarbon liquid or water suspension, is provided, for example at 46 on line 42.
  • the solid particles carried by the vaporized hydrocarbon charge make it possible to eliminate the coke, by a slight and regular erosion of the coke layer, as and when it is formed on the walls of the installation.
  • the solid particles are then separated, for the most part, from the steam cracking effluents in the cyclone 28, then reach the reservoir 34 where they are mixed with the liquid 36 to form a liquid-solid suspension.
  • the pump 38 makes it possible to recycle these particles in the installation, by recompressing the solid-liquid suspension up to a pressure level adapted to that of the injection points.
  • the solid particles which have not been separated from the gas stream in the cyclone 28 are then trapped by the liquid injected into the gas stream to effect its direct quenching.
  • solid particles having an average size of less than approximately 150 ⁇ m are useful, the rate of solid particles in the gas stream being less than 10% by weight, relative to the gas.
  • particles having average dimensions of between 5 and 85 ⁇ m, or better still between 15 and 60 ⁇ m are used, with a solid-gas ratio of between 0.1 and 8%, for example between 0.1%. and 3%.
  • the "average size" of the particles is for example such that 50% by mass of the particles have a diameter less than this dimension.
  • substantially spherical particles for example of silica-alumina, such as particles of already used catalytic cracking catalyst (silico-aluminates, produced by atomization).
  • cracking catalyst particles (silico-aluminates, zeolites), of substantially spherical shape, have in fact proved to be very effective for elimination of coke and substantially harmless to the metal of the test reactor.
  • two types of particles can be used, some of which are metal particles which are coke catalysts, for example iron, steel or nickel or a nickel-containing alloy, which are relatively soft under the conditions of steam cracking, and the others of which are harder and more erosive (for example cracking catalyst or refractory and hard metal alloy).
  • metal particles which are coke catalysts, for example iron, steel or nickel or a nickel-containing alloy, which are relatively soft under the conditions of steam cracking, and the others of which are harder and more erosive (for example cracking catalyst or refractory and hard metal alloy).
  • the preheating temperature will preferably be higher than that of the local dew point (at the injection point).
  • the decoking of the installation using these particles can be continuous or discontinuous.
  • first layer of coke of relatively small thickness, for example between 0.5 and 4 mm, or preferably between 1 and 3 mm, to harden on the internal walls of the installation. fast enough.
  • This very hard layer effectively protects the metal walls of the installation.
  • the coke which would then tend to be deposited on this protective layer is eliminated progressively, by erosion by the solid particles carried by the hydrocarbon charge.
  • the carrier gas which carries the solid particles in the installation is rich in water vapor, which plays an important role in the formation of an oxide layer (essentially chromium oxide) on the surface. internal oven tubes. It is believed that this very hard oxide film also protects the metal of the tubes against erosion by solid particles according to the invention.
  • the gaseous effluents passing through the cyclone are at an intermediate temperature, generally less than approximately 600 ° C., so that the cyclone can be made of low-alloy steel, therefore inexpensive. Its efficiency of separation of solid particles is better than at high temperature, due to the lower viscosity of the gases. Finally, the separation of the solid particles is carried out at a temperature where the speed of the cracking reactions is low. It therefore does not result in secondary chemical reactions of overcracking, which would occur if the separation of the solid particles was carried out immediately at the outlet of the oven 10.
  • FIG. 3 shows another steam cracking installation according to the invention.
  • This installation is of the multi-pass coil type, the steam cracking oven 10 being equipped with tubes 52 comprising straight lengths connected to each other by elbows 54.
  • a manifold 56 joins the tubes together at the outlet of the oven 10 and is connected to an indirect quenching boiler 58.
  • a cyclone 28 receives the gaseous effluents leaving the quenching boiler and performs the separation of solid particles.
  • the particles can be injected into the installation between three points: at the inlet of the furnace 10, at the start of the last straight length of the tubes, and at the inlet of the quenching boiler 58.
  • FIG. 4 schematically represents an alternative embodiment of the means for recycling solid particles.
  • the cyclone 28 is connected in the lower part, by an isolation valve 60 to the upper inlet 62 of a tank 64 comprising means 66, for example a vibrating screen, for separating and retaining solid particles. coarse, as well as an orifice 68 for evacuating these particles (inspection hatch).
  • the lower part of the reservoir 64 in which the fine solid particles collect, is connected by a motorized rotary member 70, of the screw or rotary lock type or the like, and by an isolation valve 72 at the inlet of another reservoir 74, the outlet of which, in the lower part, comprises a motorized rotating member 76 and an isolation valve 78, which are identical to the member 70 and to the valve 72 mentioned above.
  • the outlet of the reservoir 74 is connected by the valve 78 to a conduit 80 for recycling solid particles in the steam cracking installation.
  • a source 82 of pressurized gas supplies the conduit 80 with a gas flow at medium speed or relatively low (for example a flow of superheated steam, circulating at 20 m / s).
  • a three-way valve 84 makes it possible to connect the reservoir 74, either to the source of pressurized gas 82, or to the conduit 30 for leaving the cyclone. Stop valves 86 and 88 are provided in the conduits connecting the three-way valve 84 to the source of pressurized gas 82 and to the conduit 30, respectively.
  • An independent reservoir 90 filled with new solid particles of determined average particle size, allows, by means of a motorized rotating member 92 and an isolation valve 94, to inject an addition of solid particles into the conduit 80
  • the upper part of the reservoir 90 is connected to the outlet of this reservoir by a conduit 96 carrying out pressure balancing.
  • the rotating member 92 makes it possible to regulate the flow of the auxiliary particles.
  • the first reservoir 64 (or the reservoir 74) can be provided, in the lower part, with a purge conduit 98 making it possible to withdraw a certain quantity of used solid particles, while a conduit 100 for controlled inlet of dam gas opens out at the top of the tank 64.
  • the barrier gas is free of heavy aromatics and can be water vapor. It makes it possible to avoid coking of the reservoir 64 and of the screen 66, by avoiding the presence of cracked gases.
  • the lower reservoir 74 which had previously been filled with solid particles coming from the upper reservoir 64, is gradually emptied of its solid particles which are reinjected into the conduit 80.
  • the downstream isolation valve 78 of this reservoir is open, the rotating member 76 is rotated, and the internal volume of the reservoir 74 is connected to the pressurized gas source 82 via the valve 84, the lower stop valve 86 being open.
  • the gas delivered by the source 82 is at a pressure which is at least equal to or slightly greater than the pressure at the point of injection of the solid particles in the installation, and which is greater than the pressure in the outlet duct 30 of the cyclone 28.
  • the internal pressure of the reservoir 74 is therefore increased, relative to that of the upper reservoir 64, and is in equilibrium with the pressure in the recycling conduit 80.
  • the source 82 delivers in this conduit a gas flow at relatively speed low between 5 and 25 meters per second, for example superheated water vapor circulating at a speed between 10 and 20 meters per second, which allows solid particles in diluted gas suspension to be transported to at least one point injection into the installation.
  • the driving member 76 ceases to be driven, the valve 78 is closed, the tank 74 is connected to the cyclone outlet conduit 30 via the three-way valve 84
  • the reservoir 74 is then at the same pressure as the upper reservoir 64, and it suffices to open the isolation valve 72 and to drive the rotating member 70 so that the solid particles contained in the reservoir 64 can be transferred to the reservoir 74.
  • the purge duct 98 makes it possible to remove a stream of solid particles from the tank 64, a stream consisting of a mixture of abrasive particles coming from the booster tank and having undergone a certain attrition due to their circulation in the installation and by coke particles detached from the internal walls of the installation.
  • the two reservoirs 64, 74 are arranged in parallel between the outlet of the cyclone 28 and the recycling conduit 80 and are used alternately to respectively store the solid particles leaving the cyclone and inject them into the conduit 80.
  • a shutter valve 101 provided at the outlet of the cyclone 28 makes it possible to supply particles to one or the other reservoir.
  • the solid particles can be recycled in the installation at the inlet of the duct 26, at the inlet of the indirect quench boilers 16, as well as in line 24 for cleaning the charge vaporization pipe, located in part 22 of the furnace 10 (for example when the charge is completely vaporized, and before it is mixed with the steam).
  • This regulation of the actual pressure drop corrected in the furnace tubes corresponds to a regulation of the thickness of the coke layer maintained on the internal walls of the tubes, this thickness possibly being between 0.3 and 6 mm for example, preferably between 0.5 and 4 mm, or better between 1 and 3 mm, to protect the tubes against the risks of erosion by solid particles.
  • FIG. 6 shows another alternative embodiment of the recycling means.
  • the lower outlet 32 of the cyclone 28 is connected to an axial inlet 102 of an ejector-compressor 104, a peripheral inlet 106 of which is supplied by a flow of engine gas under high pressure.
  • the annular space between the axial feed 102 and the external wall of the ejector-compressor 104 forms a nozzle for accelerating the working gas (at high pressure) supplied by the peripheral inlet 106.
  • the outlet of the ejector-compressor is connected to an injection pipe gas-solid suspension in the installation.
  • a conduit 108 also makes it possible to inject, in the lower part of the cyclone 28, an auxiliary gas flow q + q 'to form a gas-solid suspension at the outlet of the cyclone 28.
  • the ejector-compressor 104 takes from the cyclone 28 the flow q of auxiliary gas necessary to form the gas-solid suspension.
  • the surplus q 'of auxiliary gas injected into the cyclone leaves it at the top, with the gas flow Q entering the cyclone.
  • the recompression of the gas-solid suspension which is carried out by the ejector-compressor 104 is sufficient to compensate for the pressure losses between the injection points in the installation and the entry point in the ejector-compressor 104.
  • the auxiliary gas which feeds the ejector-compressor can be water vapor, or else a heavy gas having a chemical composition such that the speed of sound in this gas is notably lower than the speed of sound in steam d 'water. It is thus possible to limit the speed of the flow in the ejector, which is linked to the speed of sound, and therefore limit the erosion of the ejector. This gas will however be chosen devoid of heavy aromatics which would increase the coking of the oven after recycling.
  • the auxiliary gas can for example be composed, for the most part, of fractions of the pyrolysis effluents recycled after hydro-treatment, boiling in the range of C4 and of the pyrolysis gasoline.
  • the ejectocharger can also be of the conventional type (central axial supply of engine gas), and constructed of abrasion-resistant materials (internal ceramic or carbide coating). A filtration of heavy particles can advantageously be made at the inlet of this ejectocompressor.
  • FIG. 7 schematically represents means of distribution or distribution of solid particles in the tubes 12 of the steam cracking furnace.
  • These tubes 12 are parallel rectilinear tubes of small diameter, the ends of which are connected to a supply manifold 14 and to an outlet collector (not shown), which may be located after a primary quench exchanger.
  • the collector 14 is supplied by the charge of vaporized hydrocarbons and water vapor which is, for example, at a temperature of the order of 550 ° C. and into which a small quantity of solid particles of small particle size is injected which are stored in the form of a suspension in a liquid such as water or light or medium hydrocarbons, in a tank 110.
  • a pump 112 makes it possible to take the liquid-solid particles mixture from the tank 110 to inject it upstream of the collector 14, in a conduit 114 in which the charge of vaporized hydrocarbons and water vapor circulates.
  • the tubes 12 of the furnace form one or more parallel rows and emerge at regular intervals into the collector 14, the latter having a section which decreases progressively from its upstream end to its downstream end relative to the direction of flow of the charge, to maintain a minimum speed of the mixture in the collector and to avoid particle deposits.
  • each tube 12 opening into the manifold 14 comprises a supply nozzle 116 extending inside the manifold and having an inlet section or an orifice 118 oriented towards the upstream end of the manifold and having a significant component in a plane perpendicular to the mean direction of flow of the charge in the collector.
  • Each tube 12 comprises, immediately downstream of the supply nozzle 116, a section restriction 120 such as a neck or a venturi, making it possible to standardize and make the gas flows in the tubes 12 substantially constant.
  • a sonic venturi is used to use a sonic venturi.
  • the downstream end 122 of the manifold 14 is connected by a duct 124 of suitable dimensions, to an ejector-compressor 126 comprising an axial duct 128 for supplying a flow of engine gas such as water vapor.
  • a valve 130 makes it possible to adjust the flow rate of engine gas.
  • the outlet of the ejector-compressor 126 is connected by a pipe 132 to the upstream end of the manifold 14 or to the pipe 114 for supplying the hydrocarbon charge.
  • the valve 130 for adjusting the flow rate of the engine gas can be controlled by a system 134 comprising means for detecting the skin temperature of the first and last tubes 12 of the furnace to control the flow of engine gas unlike these temperatures.
  • This device works as follows: The charge of vaporized hydrocarbons and water vapor, charged with solid particles of small particle size, flows with a high turbulence in the collector 14.
  • the average flow speed in this collector is between 20 and 120 meters per second, for example between 30 and 80 meters per second and is notably lower than the speed of circulation in the tubes 12, which is between approximately 130 and 300 meters per second, in particular between 160 and 270 meters per second.
  • This flow speed in the collector 14 is sufficient to avoid any gas-solid segregation in the collector and therefore any deposit of solid particles in the collector, with the possible exception of certain heavy particles, progressing along the lower generatrix.
  • the supply of an engine gas flow (for example steam) in the ejector 126 makes it possible to take the desired fraction from the gas-solid flow in the manifold and to recompress this fraction for recycling by injection into the conduit. 114 or at the upstream end of the manifold.
  • the system 134 makes it possible to adjust the flow rate of engine gas by action on the valve 130, which makes it possible to influence the supply of solid particles from the first tubes relative to the last tubes and therefore from correct an irregularity in distribution, detected by differences between the skin temperatures of these tubes.
  • the solid particles which circulate in the tubes 12 have an erosive action on the coke layer which forms on the internal wall of these tubes.
  • the variations in the skin temperature of the tubes make it possible to assess the degree of fouling of the tubes, and therefore the effectiveness of the erosion of the coke layer by the solid particles.
  • the increase in the sampling rate leads to an increase in the average speed in the collector, greater at the downstream end of the collector than at its start. The sampling rate at the end of the collector can therefore be adjusted, depending on the information on the relative fouling of the different tubes. More simply, we can set it to an adequate value.
  • the section restrictions 120 formed at the upstream end of the tubes 12 have the effect of standardizing and making substantially constant the gas flow rates which circulate in these tubes. This results in a possibility of automatic regulation of the cleaning of these tubes by solid particles. In fact, if a tube clogs abnormally, with partial obstruction by coke, the maintenance of the supply gas flow provided by the elements 120 will lead to increasing the speed of circulation and therefore the erosive efficiency.
  • a dummy supply nozzle 136 placed upstream of the first tubes 12 and which is identical to the supply nozzles 116 of these tubes.
  • the first tubes 12 will therefore be, from an aerodynamic point of view, in the same situation as the following tubes.
  • the end piece 116 is identical to those shown in FIG. 7, but the section restriction 120 is formed by a venturi with preferably sonic neck.
  • This venturi is formed from a particularly hard material to resist erosion, for example tungsten carbide or silicon carbide.
  • each tube 12 ends with an end 138 cut at a bevel, which forms the inlet end of the gas-solid particle flow rate in the tube.
  • each feed end piece is constituted by an elbow 140 at 90 °, fixed on the internal wall of the manifold 14 and into which the end of the corresponding tube 12 opens, comprising the section restriction 120.
  • the tubes 12 can be the furnace tubes, or the flexible conduits (pig tails) supplying the furnace tubes.
  • FIG. 11 shows another alternative embodiment of a steam cracking installation according to the invention.
  • the steam cracking oven 10 comprises a series of rectilinear tubes 12 of small diameter, fed at their upstream ends by a manifold 14 located outside the oven and joined at their downstream ends by a manifold 158, possibly insulated, located inside the furnace 10.
  • the manifold 158 feeds a tube 160 of larger diameter, rectilinear, the outlet end of which is connected outside the furnace to a boiler 162 for indirect quenching of the gaseous steam-cracking effluents.
  • the outlet of the boiler 162 is connected to means 164 for direct quenching of the gaseous effluents.
  • the particles injected are recovered between the boiler 162 and the quenching means 164, by means not shown.
  • the steam cracking charge consisting of a mixture of hydrocarbons and water vapor
  • the collector 14 circulates in the small tubes 12, then circulates in the opposite direction in the tube 160 of larger diameter, leaves the oven to pass through the indirect quenching exchanger 162 and reaches the means 164 for direct quenching, after recovery of the particles.
  • This installation is of the "split coil” type with two passes.
  • conduits 166 for injecting water vapor, or a water vapor-hydrogen mixture are connected to the upstream ends of the small tubes 12, outside the oven 10.
  • Each conduit 166 comprises a valve or other similar means 168 for opening and closing, and is connected to a means 170 for supplying water vapor, or a water-hydrogen mixture.
  • the valves 168 of the various conduits 166 are connected to a means 172 of sequential opening and closing control, so that only one valve 166 or a very small number of valves can be opened at a time, the other valves being closed.
  • the flow rate of water vapor or of water vapor-hydrogen mixture injected into a small tube 12 is adjusted so that it opposes the entry of the steam cracking charge into this tube.
  • the installation also includes means for injecting erosive solid particles at the upstream end of the large tube 160, preferably at the upstream ends of the manifold 158 supplying this large tube. These means are shown diagrammatically in the drawing and designated by the reference 174.
  • Another substantially equivalent possibility consists in injecting the particles into the inlet collector 14 or upstream of this collector. In this case, it is possible first of all to partially decoke the tubes 12 by means of the solid particles, and to terminate the decoking by injecting steam.
  • a gas 178 which is cooler than the gaseous steam cracking effluents, so as to pre-quench these effluents, limited to about 150 ° C, and for example between 50 and 130 ° C.
  • the pre-quench gas may be cooled cracked ethane, or optionally recycled pyrolysis gas, preferably hydro-treated, for example C5 or C6 fractions having a low octane number after extraction of the benzene.
  • Pre-quenching avoids or limits post-cracking of the effluents at the outlet of the oven 10.
  • the injection of water vapor into the tubes 12 of the oven makes it possible to decoke these tubes by a reaction of gas with water.
  • the steam leaving the tubes 12 at their downstream ends mixes in the manifold 158 with the steam cracking charge.
  • This sequential decoking of the tubes 12 of the first pass of the oven is therefore done without specific consumption of water vapor since this water vapor is recovered and used as dilution vapor in the second pass 160 of the oven.
  • the valves 168 are sequentially open, each for a determined time interval. Simultaneously or not, we can inject erosive solid particles in the collector 158 and at the inlet of the boiler 162.
  • a cyclone interposed between the quenching boiler 162 and the direct quenching means 164, makes it possible to separate the erosive solid particles from the stream of gaseous effluents.
  • the method according to the invention is perfectly suited to single-pass cracking installations, using small straight tubes, without bends, as described in FIGS. 2 and 10.
  • FIG. 11 shows that the invention can also be perfectly adapted to an installation with two or more passes, without risk of erosion at the level of the changes of direction (quantities of particles reduced or zero at this level).
  • the invention can also be used in coil installations, in particular by using a hardened coke precoat and good control of particle injections.
  • the invention therefore makes significant progress for the steam cracking industry.

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Claims (21)

  1. Verfahren zum Entkoken einer Anlage zum Dampfcracken von Kohlenwasserstoffen, das in der Entfernung durch Erosion von zumindest einem Teil des auf den Innenwänden der Anlage, im besonderen in einem Ofen (10) zum Dampfcracken und einem Kühler (16, 58) zum indirekten Abschrecken, abgelagerten Koks mittels von einem Trägergas mit hoher Geschwindigkeit transportierten Feststoffpartikeln besteht, dadurch gekennzeichnet daß die Entkokung durchgeführt wird, während die Anlage zum Cracken von Kohlenwasserstoffen betrieben wird, das Trägergas zumindest zu einem Teil vom Kohlenwasserstoff-Einsatzstoff und von Wasserdampf gebildet wird und Feststoffpartikel mit einem mittleren Durchmesser von unter 150 µm mit einem Verhältnis Feststoff-Gas von weniger als 10 Gew.-% enthält mit einer Partikelgeschwindigkeit im Ofen von 70 bis 480 m/s, so daß sich das Gemisch Trägergas-Feststoffpartikel wie ein mit einer leichten Erosionskapazität versehenes Gas verhält.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß am Ausgang des Ofens (10) zum Dampfcracken die Mischung Trägergas-Feststoffpartikel auf eine Zwischentemperatur von weniger als etwa 600 °C abgekühlt wird, die festgelegt ist, um jede Kondensation von Flüssigkeit zu vermeiden, anschließend zumindest der größte Teil der Feststoffpartikel vom Trägergas in mindestens einem Zyklon (28) abgetrennt wird, die abgetrennten Partikel mit Wasser oder einer Flüssigkeit aus annähernd von schweren aromatischen Verbindungen aus der Pyrolyse befreiten Kohlenwasserstoffen in Kontakt bringt und durch Pumpen das Gemisch Feststoffpartikel-Flüssigkeit in die Anlage zum Dampfcracken zurückführt.
  3. Verfahren nach Anspruch 1, dadurch gekennzeichnet daß am Ausgang des Ofens (10) zum Dampfcracken die Mischung Trägergas-Feststoffpartikel auf eine Zwischentemperatur von weniger als etwa 600 °C abgekühlt wird, die festgelegt ist, um jede Kondensation von Flüssigkeit zu vermeiden, anschließend zumindest der größte Teil der Feststoffpartikel vom Trägergas in mindestens einem Zyklon (28) abgetrennt wird, die den Zyklon verlassenden Partikel in mindestens einem Vorratsgefäß gesammelt werden, das gesamte Vorratsgefäß abgetrennt wird, es mittels eines Gases unter Druck gesetzt wird und zumindest ein Teil der Partikel mittels des besagten Gases in die Anlage zum Dampfcracken zurückgeführt wird.
  4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der mittlere Durchmesser der Feststoffpartikel zwischen einschließlich etwa 5 und 100 µm liegt und des Verhältnis Feststoff/Gas zwischen einschließlich 0,01 und 10 Gew.-% liegt.
  5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß der Durchmesser der Feststoffpartikel zwischen einschließlich etwa 5 und 85 µm und das Verhältnis Feststoff/Gas zwischen einschließlich 0,1 und 8 Gew.-% liegt und die Geschwindigkeit der Partikel im Ofen zwischen einschließlich 130 und 300 m/s liegt.
  6. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß die in die Anlage eingeführten Feststoffpartikel an mehreren Stellen derselben eingeblasen werden, im besonderen in einer oder mehreren Zonen des Ofens (10) zum Dampfcracken oder am Eingang des Kühlers (16, 58) zum indirekten Abschrecken oder aufeinanderfolgend in den Dampf zur Verdünnung, um eine Entkokung der Konvektionszone zu erhalten.
  7. Verfahren nach einem der Ansprüche 2, 4 bis 6, dadurch gekennzeichnet, daß die Flüssigkeit eine Fraktion des zu crackenden Kohlenwasserstoff-Einsatzstoffs oder ein Pyrolysebenzin ist.
  8. Verfahren nach einem der Ansprüche 2, 4 bis 7, dadurch gekennzeichnet, daß, um die Flüssigkeit mit den den Zyklon (28) verlassenden Feststoffpartikeln in Kontakt zu bringen, eine kontinuierliche Strömung der Flüssigkeit erzeugt wird, ausgehend von einer Quelleitung auf eine Wand, die um die und unter der Eintrittszone der Partikel liegt, um eine nasse Wand zu erzeugen.
  9. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß die Feststoffpartikel annähernd kugelförmig sind, wie zum Beispiel mineralische Partikel oder metallische Partikel, die durch Versprühen mit Gas gebildet wurden.
  10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, daß die Partikel poröse mineralische Partikel auf der Grundlage von Silikat oder Aluminat sind, wie zum Beispiel Partikel von verbrauchten Katalysatoren zum katalytischen Cracken.
  11. Verfahren nach einem der vorhergehenden Ansprüchen, dadurch gekennzeichnet, daß die Feststoffpartikel ein Gemisch sind, das zwei Partikeltypen umfaßt, wobei die einen unter den Bedingungen des Dampfcrackens relativ weiche metallische Verkokungskatalysatorpartikel und die anderen härter und stärker erosiv sind.
  12. Anlage zum Dampfcracken von Kohlenwasserstoffen, die einen Dampfcrackofen (10) mit Rohren (12) zum Durchfließen eines Kohlenwasserstoff-Einsatzstoffs, Mittel zur Einführung des besagten Einsatzstoffes und von Wasserdampf, die mit dem besagten Rohr des Ofens verbunden sind, Mittel (16, 58) zum indirekten Abschrecken der gasförmigen, den Ofen verlassenden Austragsstoffe und Mittel zum direkten Abschrecken durch Einspritzen von Flüssigkeit, die mit dem Ausgang der Mittel zum indirekten Abschrecken verbunden sind, umfaßt, dadurch gekennzeichnet, daß sie Mittel zum Einblasen von Feststoffpartikeln in den verdampften, in der Anlage während ihres Betriebs fließenden Kohlenwasserstoff-Einsatzstoff umfaßt, die mit dem besagten Rohr verbunden sind, und Mittel, wie zum Beispiel einen Zyklon (28), Abtrennung der Feststoffpartikel und des Gases, die am Ausgang der Mittel (16, 58) zum indirektem Abschrecken stromaufwärts der Mittel zum direkten Abschrecken vorgesehen sind.
  13. Anlage nach Anspruch 12, dadurch gekennzeichnet, daß sie Mittel umfaßt, um die vom Gas abgetrennten Feststoffpartikel in die Anlage zurückzuführen und Mittel für zusätzliche Feststoffpartikel.
  14. Anlage nach Anspruch 13, dadurch gekennzeichnet. daß die Mittel zum Zurückführen der Feststoffpartikel Mittel (108) zum Einblasen einer Gasmenge, die von schweren Aromaten befreit ist, in den unteren Teil der Mittel zum Abtrennen (28) umfassen, um am Ausgang dieser Mittel eine Suspension Gas-Feststoff zu erzeugen, und eine Strahlpumpe (104), die mit dem Ausgang der besagten Mittel zum Abtrennen (28) verbunden ist und mit einer Menge an Hilfsgas unter höherem Druck versorgt wird, um die Suspension Gas-Feststoff im Hinblick auf ihr Einblasen in die Anlage wieder zu komprimieren.
  15. Anlage nach Anspruch 13, dadurch gekennzeichnet, daß sie ein Vorratsgefäß (74) zur Lagerung der Feststoffpartikel umfaßt, dessen Eingang an den Ausgang (32) der Feststoffe aus den vorgenannten Mitteln (28) zum Abtrennen angeschlossen ist, und dessen Ausgang an Mittel (80) zum Einblasen der Partikel in die Anlage angeschlossen ist, Mittel (72, 78) zum Abtrennen dieses Vorratsgefäßes (74) wie z. B. Ventile und Mittel (84) zum Verbinden dieses Vorratsgefäßes mit einer Quelle (82) von Gas unter Druck, die es erlaubt, den Innendruck im Vorratsgefäß (74) auf einen Wert zu erhöhen, der mindestens gleich demjenigen am Einblaspunkt der Partikel in die Anlage ist.
  16. Anlage nach Anspruch 15, dadurch gekennzeichnet, daß sie ein zweites Vorratsgefäß (64) umfaßt, das parallel zu dem ersten genannten Vorratsgefäß (74) oder zwischen dem Ausgang der Mittel zum Abtrennen (28) und dem Eingang des ersten Vorratsgefäßes (74) angebracht ist, Mittel (60, 72) wie z. B. Ventile und Mittel (66) zum Zurückhalten von großen Partikeln, die im Inneren des zweiten Vorratsgefäßes (64) vorgesehen sind, und dadurch, daß die Quelle (82) von Gas unter Druck mit der Leitung (80) zum Einblasen der Partikel in die Anlage verbunden ist.
  17. Anlage nach einem der Ansprüche 12 bis 16, die einen Verteiler (14) zur Versorgung der Rohre (12) des Dampfcrackofens (10) umfaßt, dadurch gekennzeichnet, daß sie Mittel zum Einblasen von Feststoffpartikeln in den verdampften Kohlenwasserstoff-Einsatzstoff stromaufwärts oder am Eingang des Verteilers (14), mit einer ausreichenden Geschwindigkeit, um jegliche Ablagerung der Feststoffpartikel im Verteiler zu vermeiden, am Ende der Rohre (12) angebrachte Versorgungsstutzen (116), die sich ins Innere des Verteilers (14) erstrecken, wobei jeder Stutzen einen Eingangsabschnitt (118) umfaßt, der zum stromaufwärts gelegenen Ende des Verteilers ausgerichtet ist und der in einer senkrechten Ebene zur mittleren Strömungsrichtung im Verteiler ein Bauteil besitzt, umfaßt.
  18. Anlage nach Anspruch 17, dadurch gekennzeichnet, daß sie Mittel (124, 126, 137) zum Abscheiden von Feststoffpartikeln am stromabwärts gelegenen Ende des Verteilers umfaßt.
  19. Anlage nach Anspruch 18, dadurch gekennzeichnet, daß sie Mittel (124, 126) am stromabwärts gelegenen Ende des Verteilers zur Entnahme einer Fraktion der in den Verteiler fließenden Menge Gas-Feststoffpartikel und Mittel stromabwärts oder am Eingang des Verteilers zur Rückführung der entnommenen Fraktion der Menge Gas-Feststoffpartikel umfaßt.
  20. Anlage nach einem der Ansprüche 12 bis 19, dadurch gekennzeichnet, daß sie Mittel (142) zur Messung des Druckverlusts in den Rohren des Dampfcrackofens, Mittel (146) zur Messung des Durchsatzes an zu crackendem Einsatzstoff oder an verdünnenden Wasserdampf, Mittel (144) zur Korrektur des Druckverlusts in Abhängigkeit von diesem gemessenen Durchsatz und Mittel (148) zur Regelung des korrigierten Druckverlusts durch Regelung der Menge in die Anlage zurückgeführter Feststoffpartikel umfaßt.
  21. Anlage nach einem der Ansprüche 12 bis 20, bei der der Ofen (10) zum Dampfcracken mehrere Durchgänge für einen Kohlenwasserstoff-Einsatzstoff und Wasserdampf besitzt, mindestens ein Durchgang besteht aus einer Reihe von Rohren (12) mit kleinem Durchmesser, die von einem Sammler (158) in ein Rohr (160) mit größerem Durchmesser zusammengeführt werden, das den letzten Durchgang darstellt, die besagte Anlage umfaßt außerdem Leitungen (166) zum Einblasen von Wasserdampf, die mit den stromaufwärts gelegenen Enden der Rohre (12) mit kleinem Durchmesser verbunden sind und Instrumente (168) umfassen, wie zum Beispiel Ventile zum Öffnen und Schließen dieser Leitungen, Mittel (172) zur Steuerung dieser Instrumente, die es erlauben, ein Rohr (12) mit keinem Durchmesser nach dem anderen durch Einblasen von Wasserdampf in diese Rohre zu entkoken und Mittel (174) zum Einblasen der erosiven Feststoffpartikel in den Sammler (158), der die Rohre mit kleinem Durchmesser mit dem Rohr (160) mit großem Durchmesser verbindet.
EP90907094A 1989-04-14 1990-04-13 Verfahren und apparat zur entkoksung von dampfkrackanlagen Expired - Lifetime EP0419643B1 (de)

Applications Claiming Priority (11)

Application Number Priority Date Filing Date Title
FR8904986 1989-04-14
FR8904986A FR2645873B1 (fr) 1989-04-14 1989-04-14 Procede de decokage d'une installation de vapocraquage d'hydrocarbures, et installation de vapocraquage correspondante
FR8909373 1989-07-12
FR8909375 1989-07-12
FR8909373A FR2649717B1 (fr) 1989-07-12 1989-07-12 Procede et dispositif de decokage d'une installation de vapocraquage d'hydrocarbures
FR8909375A FR2649761B1 (fr) 1989-07-12 1989-07-12 Procede et dispositif de repartition d'un debit gazeux charge de particules solides
FR8913070 1989-10-06
FR8913070A FR2652817B1 (fr) 1989-10-06 1989-10-06 Procede et installation de vapocraquage d'hydrocarbures, a recyclage de particules solides erosives.
FR8914118 1989-10-27
FR8914118A FR2653779B1 (fr) 1989-10-27 1989-10-27 Procede de decokage d'une installation de vapocraquage d'hydrocarbures et installation correspondante.
PCT/FR1990/000272 WO1990012851A1 (fr) 1989-04-14 1990-04-13 Procede et appareillage pour le decokage d'une installation de vapocraquage

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EP0419643A1 EP0419643A1 (de) 1991-04-03
EP0419643B1 true EP0419643B1 (de) 1994-11-30

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US5186815A (en) 1993-02-16
ATE114705T1 (de) 1994-12-15
CA2030790C (fr) 2001-02-13
CA2030790A1 (fr) 1990-10-15
BR9006717A (pt) 1991-08-06
CN1046345A (zh) 1990-10-24
EP0419643A1 (de) 1991-04-03
KR920700276A (ko) 1992-02-19
KR0158203B1 (ko) 1998-12-15
DK0419643T3 (da) 1995-05-08
ES2067741T3 (es) 1995-04-01
DE69014522T2 (de) 1995-04-13
DE69014522D1 (de) 1995-01-12
WO1990012851A1 (fr) 1990-11-01
JP2845621B2 (ja) 1999-01-13
CN1024283C (zh) 1994-04-20
JPH03505604A (ja) 1991-12-05

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