Classifications

• • 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 
  • F23C10/00—Fluidised bed combustion apparatus
  • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
• • 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
  • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
  • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J29/00—Catalysts comprising molecular sieves
  • B01J29/90—Regeneration or reactivation
• • 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
  • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
  • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
  • C10G11/182—Regeneration
• • 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 
  • F23C10/00—Fluidised bed combustion apparatus
  • F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
• • 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 
  • F23C10/00—Fluidised bed combustion apparatus
  • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
  • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
  • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
  • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/70—Catalyst aspects
  • C10G2300/708—Coking aspect, coke content and composition of deposits
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/80—Additives
  • C10G2300/805—Water
  • C10G2300/807—Steam
• • 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
  • F23C2900/99008—Unmixed combustion, i.e. without direct mixing of oxygen gas and fuel, but using the oxygen from a metal oxide, e.g. FeO
• • 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
• • 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
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P30/00—Technologies relating to oil refining and petrochemical industry
  • Y02P30/40—Ethylene production

Definitions

• the invention relates to a petroleum hydrocarbon conversion plant coupled to an integrated combustion plant comprising a capture of carbon dioxide.
• Such a petroleum hydrocarbon conversion plant comprises an enclosure in which a catalytic cracking of hydrocarbons is carried out in the presence of fluidized phase catalyst particles and from which fractional petroleum fractions are recovered by ballistic separation of the particles and of these fractional petroleum fractions.
• a regenerator of the catalyst particles At this first chamber is conventionally associated a regenerator of the catalyst particles, on which coke is deposited in the cracking chamber. In this regenerator, the catalyst particles are regenerated by combustion of the coke and are then recycled to the feed of the cracking vessel.
• This capture of carbon dioxide can be carried out in a reactor by washing with a solvent, for example monoethanolamine, which selectively solubilizes the carbon dioxide.
• the solvent is then regenerated by extracting the carbon dioxide by heating by injecting steam into another reactor and the regenerated solvent is returned to the washing reactor.
• this solution makes it necessary to treat the nitrogen, which is also discharged with the carbon dioxide at the top of the catalyst regenerator, which makes it necessary to size the carbon dioxide capture plant in proportion to the amount of nitrogen. present.
• thermal regeneration has the disadvantage of requiring large amounts of steam. This solution is therefore very energy consuming. It can therefore be envisaged to replace the nitrogen diluent with recycled carbon dioxide and to carry out the combustion with an O 2 / CO 2 oxidant.
• oxygen is produced from air through an air separation unit by a cryogenic system that consumes a lot of energy. It is also known to carry out a combustion of gas with integrated carbon dioxide recovery by using a metal oxide serving as an oxygen carrier vector. This oxide circulates between two reactors in which it is either oxidized in a circulating fluidized bed reactor by contact with air, or reduced by contact with the gaseous fuel. This method has the advantage of not requiring an air separation unit since the oxide constitutes the oxygen carrier.
• This type of combustion plant of carbonaceous solids operating at atmospheric pressure with integrated capture of carbon dioxide does not require prior separation of the air. Because of its simplicity and compactness, this system reduces the costs of capturing carbon dioxide while ensuring the production of steam for the generation of electricity.
• the invention proposes an integration of a system of this type in the capture of the carbon dioxide emitted in a hydrocarbon conversion plant as specified above. Thanks to the invention, the carbon dioxide is captured, while ensuring the production of steam for the production of energy, and this at an optimal cost and bulk.
• the invention provides a petroleum hydrocarbon conversion plant comprising a catalytic cracking chamber in the presence of fluidized phase catalyst particles and a regenerator of said catalyst particles by combustion of coke deposited thereon, said catalyst circulating between said cracking chamber and said regenerator, said regenerator being a reactor integrated into a combustion plant for the production of steam comprising a capture of carbon dioxide, characterized in that said regenerator is a reactor for reducing a carrier of carbon dioxide, oxygen, fed with solid fuel comprising said particles provided with coke and equipped with a cyclone for separating solids and exchangers, this reduction reactor of said oxygen carrier being associated with an oxidation reactor of said oxygen carrier and equipped with a cyclone separating solids and exchangers, said oxygen carrier circulating between these two reactors and in that said oxygen carrier consists of oxide particles metal of different average diameter from that of said catalyst particles.
• said oxygen carrier may consist of said catalyst particles.
• said oxygen support consists of particles of metal oxides of average diameter different from that of said catalyst particles.
• said reduction reactor is a circulating fluidized bed fluidized with steam and / or recycled carbon dioxide and / or sulfur dioxide.
• the plant comprises at the outlet of the cyclone of the reduction reactor a siphon separating said metal oxide particles directed towards the oxidation reactor and said catalyst particles directed towards the cracking chamber.
• said granulometric sorter consists of a circulating fluidized bed equipped with a separation cyclone.
• said catalyst particles are reinjected into said cracking chamber by means of an ascending pipe of a determined height whose pressure drop compensates for the pressure difference between said chamber and said particle size sorter.
• the pressure difference between the circulation loop of the catalyst particles and the circulation loop of the metal oxide particles is balanced.
• the ratio between the mean diameter of the metal oxide particles and that of the catalyst particles is advantageously greater than two.
• the said metal oxides may comprise iron oxide.
• Said catalyst particles may comprise nickel oxide.
• said solid fuel also contains petroleum residues, such as pitches, bitumen or asphalt, so as to generate sufficient useful power.
• This figure represents an installation according to the invention.
• This facility includes a petroleum hydrocarbon conversion facility with a catalytic cracker
• the regenerator 2 is an integrated reactor in a combustion plant for the production of steam comprising a capture of carbon dioxide.
• This regenerator 2 is a reactor for reducing an oxygen carrier, preferably consisting of particles of metal oxides of average diameter different from that of the catalyst particles, supplied with solid fuel comprising the particles provided with coke by the supply line 1A and equipped with a separation cyclone C2 solids and exchangers E2.
• the solid fuel supplied by line A2 may also include petroleum residues.
• This reduction reactor is a circulating fluidized bed furnace fluidized with water vapor by a feed pipe 2B and a wind box 2C for introducing the fluidization vapor at the bottom of the reduction reactor 2 To this water vapor is mixed carbon dioxide or recycled sulfur dioxide by a complementary conduit 2D opening into the same wind box 2C.
• the temperature is of the order of 900 ° C. and the pressure is of the order of atmospheric pressure.
• this reduction reactor 2 is a circulating fluidized bed fluidized with water vapor and / or recycled carbon dioxide and / or sulfur dioxide.
• the cyclone C2 In the upper part of the reduction reactor 2 is installed the cyclone C2 where the solid particles are separated from the fly ash and combustion gases consisting of carbon dioxide, sulfur dioxide and water vapor.
• Fly ash and combustion gases are fed to the steam generators E2 heat exchangers for example the generation of electricity. Fly ash is separated from the flue gases in an F2 bag filter. The combustion gases are then sent to a cooling and condensation circuit R2 via a fan V2. This circuit makes it possible to extract the water and the remaining H 2 SO 4 from the carbon dioxide which is then partially reintroduced into the reactor 2 via the complementary conduit 2D. The fly ash is separated from the metal oxide particles by an S2 particle size separator to be stored in a silo, while the metal oxide particles are directed to a silo 4.
• the solid particles at the outlet of the separator C2 consisting of particles of metal oxides, regenerated catalyst particles and carbon residues, pass through a siphon 5 where a first part is sent in a particle size separator 6 for the separation of the metal oxide particles and catalyst particles and which will be specified below.
• a second portion at the outlet of the cyclone is directed towards a device for removing the carbon residue 7.
• This elimination device 7 is fluidized with water vapor via an inlet pipe 8 in water vapor, also supplying water. the feed pipe 2B of the reduction reactor 2.
• This fluidization makes it possible to separate the fine and light particles such as the carbonaceous residue from the metal oxide particles and reintroduce them into the reduction reactor 2 via a pipe 7A, while the denser and larger particles of metal oxides are transferred via line 7B to a second reactor 3 which is an oxidation reactor.
• a second reactor 3 which is an oxidation reactor.
• An example of the constitution of such an elimination device 7 is described in patent document FR 2,850,156.
• the oxidation reactor 3 is equipped with a starting system D3 which is supplied with fuel such as gas, a system for introducing the metal oxide particles from the oxide silo 4 and a fluidization and oxidation system via an air supply pipe 9.
• This starting system D3 makes it possible to reheating all the reactors and solids circulation loops to a temperature threshold above 700 ° C and launching all the reactions.
• Oxidation reactor 3 of the oxygen support here consisting of particles of metal oxides of average diameter different from that of the catalyst particles, is equipped with a cyclone for separating solids C3 and E3 exchangers.
• a bed composed of metal oxides circulates in the oxidation reactor 3 which is fluidized by air coming from the inlet pipe 9 supplying a wind box 3C.
• the temperature is of the order of 1000 ° C. and the pressure is of the order of atmospheric pressure.
• the solid particles which have been extracted under cyclone C3 pass through a siphon 11 from which a first part is transferred to the bottom of the reduction reactor 2, a second part is recirculated to the bottom of the oxidation reactor 3 and a third part is directed to an outer bed 12 which is placed a heat exchanger fluidized by air supplied by the air inlet pipe 9, and finally reintroduced into the oxidation reactor 3.
• This exchanger can regulate the temperature in the oxidation reactor 3.
• a top-up of metal oxide particles in the oxidation reactor 3 is possible via the oxide silo 4 via line 13.
• a top-up of oxide particles may be justified to compensate for attrition losses in the various reactors 2 and 3, in order to have enough oxides to ensure the transfer of materials and the circulation of solids.
• the large particles of ash or agglomerates are extracted periodically by an extraction line 14 at the bottom of the oxidation reactor to a recovery silo.
• a grain size sorter 6 reinjecting the metal oxide particles in the reduction reactor 2 and the catalyst particles in the cracking chamber 1.
• the oxygen carrier is made of metal oxide particles different from the catalyst particles, which consists for example of nickel oxide.
• This oxide metal preferably comprises iron oxide and may also comprise manganese oxide, copper oxide or nickel oxide.
• this oxygen carrier may consist of the catalyst particles, themselves.
• the grain size sorter 6 is not necessary.
• the particle size of these particles is chosen so that the ratio between the average diameter of the oxide particles and that of the catalyst particles is greater than together.
• the oxide particles have an average diameter of about 160 microns and the catalyst particles have an average diameter of about 60 microns.
• the grain size sorter 6 consists of a circulating fluidized bed 6A supplied with water vapor through the inlet pipe 8 and equipped with a separation cyclone 6B sized to perform this sorting.
• a separation cyclone 6B sized to perform this sorting.
• the oxide particles which are reinjected in the lower part of the reduction reactor 2.
• the catalyst particles are returned to the cracking chamber 1 by means of an ascending duct 6C of a determined height whose pressure drop compensates for the pressure difference between the cracking chamber 1 and the grain size sorter 6. This transfer is effected via a hopper 15.
• this reduction reactor 2 is a circulating fluidized bed, a residence time in this elongated reactor is obtained thanks to the internal circulation of the solids in this reactor and the recirculation via its cyclone C2.
• the volatile materials are released very quickly following the warming of the fuel and react with the oxygen released by the oxygen metal carrier oxides to achieve a partial combustion which is continued by the combustion of fixed carbon, ensuring on the one hand the elimination of coke carried by the catalyst particles which are regenerated, and secondly the reduction of optionally complementary metal oxide particles.
• Part of the oxide bed is extracted at the base of the siphon 5 located under the cyclone associated with this reduction reactor 2, to be purified carbon residues that have not been converted into fly ash, thanks to the elimination device 7 which constitutes a carbon barrier throughout the installation, then reintroduced into the oxidation reactor 3 to be oxidized by the oxygen of the air.
• the oxygen depleted air leaving the oxidation reactor 3 is cooled in the heat exchanger E3, which in practice consists of a plurality of exchangers, then dedusted in the bag filter F3 and returned to the atmosphere.
• the oxide particles regenerated as they pass through the oxidation reactor 3 are returned to the reduction reactor 2 to initiate a new oxygen transport cycle of the oxidation reactor 3 to the reduction reactor 2
• the amount of oxides returned to the reduction reactor 2 can be controlled by a solids flow control valve not shown.
• Another part of the oxide bed extracted at the base of the siphon 5 situated under the cyclone associated with the reduction reactor 2 is directed firstly downwards of the reduction reactor 2 in order to maintain a circulation of solids in the reactor. 2, and on the other hand to the grain size sorter 6, which makes it possible to separate the regenerated catalyst particles which are reinjected into the cracking chamber 1 and the residual oxide particles which are reintroduced at the bottom of the reduction reactor.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Combustion & Propulsion (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• General Chemical & Material Sciences (AREA)
• Materials Engineering (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Fluidized-Bed Combustion And Resonant Combustion (AREA)
• Catalysts (AREA)

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• 2005
  • 2005-12-27 FR FR0554103A patent/FR2895413B1/fr not_active Expired - Fee Related
• 2006
  • 2006-12-22 BR BRPI0621263-8A patent/BRPI0621263A2/pt not_active Application Discontinuation
  • 2006-12-22 EP EP06847204A patent/EP1969092A1/de not_active Withdrawn
  • 2006-12-22 RU RU2008130900/04A patent/RU2418843C2/ru not_active IP Right Cessation
  • 2006-12-22 CA CA2634129A patent/CA2634129C/en not_active Expired - Fee Related
  • 2006-12-22 KR KR1020087018338A patent/KR100996373B1/ko not_active IP Right Cessation
  • 2006-12-22 WO PCT/FR2006/051415 patent/WO2007074304A1/fr active Application Filing
  • 2006-12-22 CN CN2006800495169A patent/CN101351530B/zh not_active Expired - Fee Related
  • 2006-12-22 JP JP2008548018A patent/JP4851538B2/ja not_active Expired - Fee Related
  • 2006-12-22 US US12/086,659 patent/US8318101B2/en not_active Expired - Fee Related

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