EP2417391A2 - Procédé et dispositif de craquage de substances hydrocarbonées - Google Patents

Procédé et dispositif de craquage de substances hydrocarbonées

Info

Publication number
EP2417391A2
EP2417391A2 EP10711848A EP10711848A EP2417391A2 EP 2417391 A2 EP2417391 A2 EP 2417391A2 EP 10711848 A EP10711848 A EP 10711848A EP 10711848 A EP10711848 A EP 10711848A EP 2417391 A2 EP2417391 A2 EP 2417391A2
Authority
EP
European Patent Office
Prior art keywords
cracking furnace
flue gas
oxygen
heating medium
cracking
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.)
Withdrawn
Application number
EP10711848A
Other languages
German (de)
English (en)
Inventor
Gunther Schmidt
Volker Göke
Boris Banovsky
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Publication of EP2417391A2 publication Critical patent/EP2417391A2/fr
Withdrawn legal-status Critical Current

Links

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
    • 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
    • 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
    • C10G9/206—Tube furnaces controlling or regulating the tube furnaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/007—Supplying oxygen or oxygen-enriched air
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/22—Higher olefins
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/99001—Cold flame combustion or flameless oxidation processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07001—Injecting synthetic air, i.e. a combustion supporting mixture made of pure oxygen and an inert gas, e.g. nitrogen or recycled fumes
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/32—Direct CO2 mitigation
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a process for the cleavage of a hydrocarbon-containing feed into shorter-chain hydrocarbons in a plant for producing hydrocarbons (olefin plant), wherein the hydrocarbon-containing feed is guided into the cracking tubes of a cracking furnace and the long-chain hydrocarbons of the feed are thermally cracked into shorter-chain hydrocarbons, and a plant to carry out the process.
  • the invention is described using the example of an ethylene plant using steam as a diluent, but is in principle suitable for any process and any plant of the type mentioned and not limited to ethylene plants.
  • a hydrocarbonaceous feedstock (eg, naphtha) is converted to the desired shorter chain hydrocarbons by steam cracking.
  • the hydrocarbonaceous feedstock in the convection zone of a cracking furnace is preheated to 550 0 C - 650 ° C.
  • hot process steam is added to the feedstock containing hydrocarbon.
  • the gaseous mixture of hydrocarbon-containing feed and water vapor is fed from the convection zone into the heated gap tubes of the cracking furnace.
  • the process steam serves to lower the partial pressure of the individual reactants as well as to prevent a renewed juxtaposition of already split shorter-chain hydrocarbons (polymerization).
  • the residence time in the gap tubes of the cracking furnace is about 0.2 to 0.6 seconds.
  • the crevices consist of a chromium-nickel alloy and are heated in the cracking furnace mainly by thermal radiation in the so-called radiation zone.
  • the radiation zone the actual furnace of the cracking furnace, there is a temperature between 1100 0 C and 1300 0 C. This temperature is reached in the prior art by the combustion of a heating medium, usually hot gas, with air.
  • a prior art cracking furnace essentially consists of two main areas. These are the radiation zone and the waste heat zone.
  • the actual furnace of such a cracking furnace there is a temperature between 1100 0 C and 1300 0 C.
  • the cracking tubes for cleavage of the hydrocarbon-containing insert lead directly through this radiation zone.
  • the heating medium is burned with air and are in the radiation zone, the resulting heat energy, mostly by means of heat radiation, on the gap tubes and thus on a further heat transfer to the hydrocarbon-containing use.
  • the product gas is passed out of the cracking furnace in the cans for cooling and separation.
  • the radiation zone of the cracking furnace adjoins the waste heat zone on the flue gas side.
  • the cooling of the flue gases produced during the combustion of the heating medium begins.
  • the flue gas is cooled to temperatures in the range of about 120 0 C to 150 0 C, especially by a convective heat transfer with other process streams of the system.
  • the resulting during combustion flue gas thus leaves the cracking furnace with a temperature of below 150 0 C. Since the cooling of the flue gas takes place under heating of process streams in the system, very little heat of combustion of the heating medium is lost and the thermal efficiency of a cracking furnace is behind the prior art at 90% to 94% based on the lower calorific value of the fuel used.
  • the flue gases produced during combustion of the heating gas contain nitrogen oxides. These nitrogen oxides are harmful to humans and a major cause of acid rain, smog and ozone formation under UV radiation. Therefore, the most complete removal of the nitrogen oxides from the flue gas is desirable before the escape into the atmosphere.
  • the nitrogen oxides (NO x ) in the flue gas can be catalytically converted to nitrogen and water by a method of selective catalytic reduction by contacting with a catalyst (DeNO x catalyst) in the presence of a reducing agent.
  • EP 1834688 proposes a method and a device for the catalytic removal of nitrogen oxides from the flue gas of a cracking furnace.
  • a suitable catalyst is arranged directly at the cold end of the waste heat zone or in a separate reactor directly at the outlet to the waste heat zone and the nitrogen oxides are converted with hydrogen as a reducing agent to nitrogen and water.
  • the catalytic removal of the nitrogen oxides can be carried out according to another prior art at a temperature between 250 0 C and 500 0 C with ammonia as a reducing agent (eg WO02068097).
  • the present invention has for its object to develop an alternative method and an associated system that avoids the escape of nitrogen oxides with the flue gas of a cracking furnace into the atmosphere.
  • the stated object is achieved by the method in that the cracking furnace is heated by the combustion of a heating medium with pure oxygen.
  • pure oxygen is understood as meaning an oxygen-containing gas which has an oxygen content of more than 90% by volume. Preference is given to using pure oxygen having a purity of more than 99.5% by volume and a maximum of 0.2% by volume of nitrogen. Such pure oxygen combustion is also referred to as oxyfuel combustion.
  • the heating medium is not burned with air but with pure oxygen in the inventive method.
  • Air is 78% nitrogen by volume.
  • high combustion temperatures of about 1200 ° C are formed from the nitrogen of the air nitrogen oxides such as nitrogen monoxide and nitrogen dioxide in the range of 40-100 ppm.
  • the use of pure oxygen without nitrogen content, the nitrogen content in the cracking furnace and thus the amount of nitrogen oxides formed in the cracking furnace is significantly reduced.
  • the resulting flue gas is thus completely free of nitrogen oxides, which could pollute the atmosphere.
  • the method according to the invention is suitable both for cracking furnaces with pure soil firing and for blast furnaces with mixed firing (burners on the ground and on the lateral walls of the cracking furnace).
  • the nitrogen oxides in the flue gas are therefore reduced so much that the use of a catalytic nitrogen oxide removal is superfluous.
  • the use of pure oxygen significantly reduces the total amount of flue gas.
  • the process of the invention offers a number of further advantages. Due to the reduced amount of flue gas significantly more heat per heating medium in the radiation zone is absorbed than in the prior art. Due to the lower nitrogen content, the partial pressure of carbon dioxide in the combustion chamber increases. Carbon dioxide is an excellent gas emitter, so that much more energy can be transferred to the gap tubes through heat radiation. Thus, the energy efficiency of the cracking furnace is further improved and the amount of heating medium consumed per ton of value-added products produced (e.g., ethene, propene, and other high-quality chemicals) decreases. Due to the lower burned amount of heating medium produced by the novel process also significantly less carbon dioxide than in a method according to the prior art. Thus, the environmental balance per ton of produced value products is improved by the method according to the invention.
  • value-added products produced e.g., ethene, propene, and other high-quality chemicals
  • the pressure, the volumetric flow and / or the inlet velocity of the heating medium and / or the oxygen are adjusted such that the heating medium burns flaming.
  • the pressure, the volumetric flow and / or the inlet velocity of the heating medium and / or the oxygen are adjusted such that the heating medium burns flaming.
  • the pressure, the volumetric flow and / or the inlet velocity of the heating medium and / or the oxygen are adjusted such that the heating medium burns flaming.
  • the pressure, the volumetric flow and / or the inlet velocity of the heating medium and / or the oxygen are adjusted such that the heating medium burns flaming.
  • a combustion with visible flame is considered to be the region in which an exothermic reaction of gases or vapors occurs with the emission of radiation by intermediate species such as hydrocarbon radicals or soot in the visible spectral range.
  • Flameless combustion in contrast, is combustion without the formation of a visible flame. That in flameless combustion, no region forms in which gases or vapors react exothermally emitting radiation in the visible spectral range.
  • the combustion products water and carbon dioxide emit almost exclusively in the invisible to humans infrared range.
  • the pressure, the flow rate, the inlet velocity and / or the apparatus design of the inlet lances of the heating medium and / or the oxygen are adjusted so that heating gas, oxygen and recirculated flue gas are almost ideally mixed before it for the actual combustion reaction comes.
  • Combustion temperatures are assisted by stimulating internal flue gas circulation.
  • the corresponding adjustment of the parameters is known to the person skilled in the art.
  • this embodiment of the invention there is a flameless combustion.
  • This embodiment of the invention has further advantages. In a flameless combustion, the distance between the burners and the
  • Canned tubes are reduced.
  • the elimination of the reducing flame zone precludes a potentially damaging influence of the flame.
  • flameless combustion is characterized by a very uniform combustion process in the room.
  • the temperature profile of the cleavage reaction in the split tubes can be made more homogeneous.
  • a more homogeneous temperature and thus also density profile in the cracking furnace simultaneously leads to a significantly reduced noise emission.
  • the internal circulation ensures an increase in the heat transfer to the split tubes by convection.
  • the energy efficiency of the method according to the invention is further increased in this embodiment.
  • the oxygen is preferably fed to the cracking furnace at a primary pressure of at least 3 bar, more preferably between 5 bar and 6 bar.
  • a flameless combustion develops within the cracking furnace.
  • the use of a pre-pressure between 5 bar and 6 bar has the additional advantage that it can be dispensed with a pressure regulation of the oxygen, since 5 to 6 bar corresponds to the oxygen supply pressure from adjacent air separation plants.
  • flaming combustion is also possible in this embodiment of the invention.
  • At least part of the flue gas leaving the cracking furnace is returned to the furnace.
  • This embodiment of the invention is particularly suitable for retrofitting existing cracking furnaces.
  • the energy efficiency of the cracking furnace is improved so much that much less heat in the heat-recovery zone of the cracking furnace is dissipate. In existing cracking furnaces, this heat is in the
  • waste heat zone for urgently needed heating of other process streams for example, the generation of high-pressure steam
  • a conversion to the method according to the invention would therefore have a complete reorganization of the system result in old systems. This complete conversion is avoided by this embodiment of the invention. Due to the external circulation of the
  • Flue gas ie a portion of the cold flue gas with a temperature between 80 0 C and 150 0 C is returned to the heat zone of the cracking furnace back into the radiation zone and thus the furnace of the cracking furnace, the effect on the cracking furnace can be reduced to a minimum, so that no complete reorganization of the entire system is necessary.
  • the recirculated flue gas can be blown either at several points in the furnace or injected together with the oxygen through the burner.
  • the control of the flue gas circulation allows the control of the burn-out process in the cracking furnace.
  • the temperature profiles and the dependent heat flow densities of the transmission to the gap tubes can be designed. This means a higher degree of design freedom in the design of the cracking furnaces.
  • the method according to the invention it is possible to use significantly fewer burners with a higher specific power or the same number of burners with a lower specific power than in the prior art.
  • the extent of the radiation zone can be reduced because the heat input to the gap tubes is much more uniform and effective than in the prior art.
  • a plant for the production of hydrocarbons by cleavage of a hydrocarbon-containing insert in a cracking furnace the cracking furnace at least one can for guiding the hydrocarbonaceous insert through the furnace of the cracking furnace, at least one means for supplying or discharging the hydrocarbonaceous insert into the cans, at least one means for supplying the heating medium and at least one means for supplying an oxygen-containing gas, are designed such that no loaded with nitrogen oxides flue gas is released into the atmosphere.
  • the object is achieved on the device side, that the means for supplying an oxygen-containing gas is connected to a source of pure oxygen.
  • the combustion of the heating medium with pure oxygen takes place in the cracking furnace.
  • the means for supplying the heating medium and the means for supplying the oxygen are designed as Venturi nozzles. Also advantageous is the supply of heating medium, oxygen or flue gas in the cracking furnace via inlet lances.
  • the system has at least one supply for flue gases in the combustion chamber, which is fluidically connected to the withdrawal of the flue gas from the cracking furnace.
  • a suction fan for the withdrawal of the flue gas from the cracking furnace downstream of the heat recovery zone of the cracking furnace.
  • a second fan is upstream of the supply of the flue gas into the furnace of the cracking furnace. The recycled flue gas is thereby advantageously guided directly into the cracking furnace.
  • the recirculated flue gas is mixed with the oxygen.
  • the present invention has a number of advantages.
  • the nitrogen oxide content in the flue gas of a cracking furnace is significantly reduced compared to the prior art. Elaborate methods for removing nitrogen oxides from the flue gas of the cracking furnace are therefore not necessary.
  • the energy efficiency is significantly increased by means of the method according to the invention and the system according to the invention, so that significantly less carbon dioxide is produced per tonne of added value products, since a significantly smaller amount of heating medium per tonne of added value products is consumed.
  • the resulting carbon dioxide is easier to remove from the flue gas than in the prior art. Since in the flue gas according to the prior art, a significant amount of nitrogen is still present, sour gas scrubbing for carbon dioxide removal must be used. According to the method of the invention, the resulting flue gas is almost free of nitrogen. Thus, it is sufficient only to condense the water from the flue gas to obtain a pure carbon dioxide gas stream.
  • Figure 1 shows an embodiment of the invention without external flue gas circulation
  • Figure 2 shows an embodiment of the invention with external flue gas circulation
  • FIG. 3 shows a further embodiment of the invention with external flue gas circulation
  • Figure 1 shows an embodiment of the invention without external flue gas circulation.
  • the cracking furnace 1 consists of a radiation zone 1a, the actual firebox, and a waste heat zone 1b.
  • the hydrocarbonaceous feed is passed through crevice tubes (not shown) through the radiation zone.
  • the radiation zone is heated by the combustion of the heating medium 2 with pure oxygen 3.
  • Heating medium and the oxygen are fed into the burner 4. There, the mixing and combustion of the heating medium take place. Depending on the chosen pressure, volume flow and speed of heating gas and oxygen, the combustion can be flaming or flameless. For the flameless burning of the fuel gas and the generation of the necessary internal flue gas circulation, a normally existing oxygen supply pressure of 5 to 6 bar is sufficient.
  • the flue gas 5 leaves via the waste heat zone 1 b the cracking furnace.
  • the remaining heat of the flue gas 5 can also be used via an optional heat exchanger 6 for heating any process stream (for example ethane, propane, naphtha, etc.).
  • the flue gas 7 free of nitrogen oxides can then be released into the atmosphere without further measures.
  • Figure 2 shows an embodiment of the invention with external flue gas circulation.
  • the flue gas 5 is sucked by means of suction fan 8 from the waste heat zone 1 b of the cracking furnace 1.
  • a part 5a of the thereby withdrawn flue gas is returned to the furnace 1 a of the cracking furnace 1.
  • the non-recirculated portion of the flue gas 5 can be released into the atmosphere without further measures.
  • another blower (not shown) can be integrated into the external recirculation of the flue gas 5a.
  • Figure 3 shows a further embodiment of the invention with external flue gas circulation.
  • the pure oxygen 3 is fed directly into the external recirculation of the flue gas 5a.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé de craquage d'une charge contenant des hydrocarbures en hydrocarbures à chaîne plus courte, dans une installation pour produire des hydrocarbures (installation d'oléfines), la charge contenant des hydrocarbures étant conduite dans le tube de craquage d'un four de craquage (1) et les hydrocarbures à chaîne plus longue de la charge étant craqués thermiquement en hydrocarbures à chaîne plus courte. L'invention concerne également, une installation pour réaliser le procédé. Le four de craquage (1) est chauffé par la combustion d'un agent de chauffage (2) avec de l'oxygène pur (3).
EP10711848A 2009-04-07 2010-03-30 Procédé et dispositif de craquage de substances hydrocarbonées Withdrawn EP2417391A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009016695A DE102009016695A1 (de) 2009-04-07 2009-04-07 Verfahren und Vorrichtung zur Spaltung von Kohlenwasserstoffen
PCT/EP2010/002033 WO2010115561A2 (fr) 2009-04-07 2010-03-30 Procédé et dispositif de craquage de substances hydrocarbonées

Publications (1)

Publication Number Publication Date
EP2417391A2 true EP2417391A2 (fr) 2012-02-15

Family

ID=42733182

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10711848A Withdrawn EP2417391A2 (fr) 2009-04-07 2010-03-30 Procédé et dispositif de craquage de substances hydrocarbonées

Country Status (3)

Country Link
EP (1) EP2417391A2 (fr)
DE (1) DE102009016695A1 (fr)
WO (1) WO2010115561A2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4105297A1 (fr) * 2021-06-16 2022-12-21 Linde GmbH Procédé et système de mesure permettant de déterminer une teneur en oxygène dans un four, four et installation technique
EP4310160A1 (fr) 2022-07-22 2024-01-24 Linde GmbH Procédé et installation de vapocraquage

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3836131A1 (de) * 1988-10-22 1990-04-26 Linde Ag Reaktor zur durchfuehrung von verbrennungsprozessen
US5431559A (en) * 1993-07-15 1995-07-11 Maxon Corporation Oxygen-fuel burner with staged oxygen supply
DE4400831A1 (de) * 1994-01-13 1995-07-20 Messer Griesheim Gmbh Verfahren zur Reduzierung von Schadgasemissionen bei der Verbrennung und Brenner dafür
US6126438A (en) * 1999-06-23 2000-10-03 American Air Liquide Preheated fuel and oxidant combustion burner
US6821490B2 (en) 2001-02-26 2004-11-23 Abb Lummus Global Inc. Parallel flow gas phase reactor and method for reducing the nitrogen oxide content of a gas
DE102005005832B4 (de) * 2005-02-08 2006-11-02 Air Liquide Deutschland Gmbh Rekuperatorbrenner und Verfahren zum Erhitzen eines Industrieofens unter Einsatz des Brenners
DE102006012206A1 (de) 2006-03-16 2007-09-20 Linde Ag Verfahren zur Entfernung von Stickoxiden aus Rauchgasen von Verbrennungsöfen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2010115561A2 *

Also Published As

Publication number Publication date
DE102009016695A1 (de) 2010-10-14
WO2010115561A3 (fr) 2011-10-13
WO2010115561A2 (fr) 2010-10-14

Similar Documents

Publication Publication Date Title
EP2512981B1 (fr) Procédé permettant de faire fonctionner un four de reformage et installation de reformage
EP1877173B1 (fr) Procede et reacteur pour effectuer des reactions catalytiques endothermiques
DE102009053747A1 (de) Verfahren zur Reduzierung von Stickoxiden aus dem Abgas eines Koksofens
WO2008131832A1 (fr) Reformeur primaire présentant des canaux d'entrée secondaires alimentant le brûleur
DE2159790B2 (de) Verfahren und Vorrichtung zur kontinuierlichen Herstellung von Schwefeldioxid hoher Reinheit
EP2417391A2 (fr) Procédé et dispositif de craquage de substances hydrocarbonées
DE2444333A1 (de) Ofen zum cracken von kohlenwasserstoffen zum herstellen von olefinen
DE2616085A1 (de) Mit waerme arbeitender reformierofen und diesen enthaltendes reformiersystem
DE1208031B (de) Vorrichtung zur Herstellung eines Heizgases
EP3068529A1 (fr) Procédé et dispositif de reformage à la vapeur et de clivage à la vapeur d'hydrocarbures
DE102009016696A1 (de) Verfahren und Vorrichtung zur Spaltung von Kohlenwasserstoffen mit sauerstoffangereicherter Luft
WO1997026985A2 (fr) Procede de realisation d'une reaction endothermique et reacteur permettant de mettre en oeuvre ledit procede
EP0365899A2 (fr) Réacteur pour la mise en oeuvre des procédés de combustion
EP3519731B1 (fr) Procédé de réduction d'émission de nox
DD203067A5 (de) Verfahren und vorrichtung zum dampfcracken von schweren kohlenwasserstoffen
DE2437907A1 (de) Verfahren und vorrichtung zum gewinnen reduzierenden gases unter druck und bei hoher temperatur
EP3910236B1 (fr) Brûleur de processus et procédé de combustion des gaz de combustion contenant du monoxyde de carbone
DE102009048102A1 (de) Verfahren und Vorrichtung zur Reformierung von Kohlenwasserstoffen
EP2703716A1 (fr) Chauffage d'un gaz d'échappement de processus
WO2018108321A1 (fr) Échangeur de chaleur comprenant un brûleur
EP2048217A2 (fr) Procédé de décocage de fours de craquage
DE102010055453A1 (de) Brennerbefeuerter Reaktor
WO1994029491A1 (fr) Procede et dispositif de traitement thermique de pieces
DE102010024539A1 (de) Primärreformer mit variablem Rauchgasstrom
DE921263C (de) Katalytisches Regenerativverfahren und Vorrichtung zur Durchfuehrung des Verfahrens

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20110929

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20120605