US20030116471A1 - Catalytic cracking process of petroleum hydrocarbons - Google Patents

Catalytic cracking process of petroleum hydrocarbons Download PDF

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Publication number
US20030116471A1
US20030116471A1 US10/229,155 US22915502A US2003116471A1 US 20030116471 A1 US20030116471 A1 US 20030116471A1 US 22915502 A US22915502 A US 22915502A US 2003116471 A1 US2003116471 A1 US 2003116471A1
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Prior art keywords
tube
catalyst
inner tube
oil
process according
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US10/229,155
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Inventor
Ruichi Zhang
Xiaoxiang Zhong
Jiushun Zhang
Kejia Xu
Zhigang Zhang
Shuandi Hou
Xueliang Chang
Zhiguo Wu
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
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Priority claimed from CN 01258820 external-priority patent/CN2498160Y/zh
Priority claimed from CN 01264042 external-priority patent/CN2506644Y/zh
Priority claimed from CNB011414774A external-priority patent/CN1184283C/zh
Priority claimed from CNB011342692A external-priority patent/CN1184282C/zh
Priority claimed from CNB011342684A external-priority patent/CN1184281C/zh
Application filed by China Petroleum and Chemical Corp filed Critical China Petroleum and Chemical Corp
Assigned to RESEARCH INSTITUTE OF PETROLEUM PROCESSING, SINOPEC, CHINA PETROLEUM & CHEMICAL CORPORATION reassignment RESEARCH INSTITUTE OF PETROLEUM PROCESSING, SINOPEC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CHANG, XUALIANG, HOU, SHUANDI, WU, ZHIGUO, ZHANG, JUISHUN, ZHANG, RUICHI, ZHANG, ZHIGANG, ZHONG, XIAOXIANG
Publication of US20030116471A1 publication Critical patent/US20030116471A1/en
Abandoned legal-status Critical Current

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    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0025—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by an ascending fluid
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/004—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a nozzle
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • B01J8/30—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other the edge of a lower bed projecting beyond the edge of the superjacent bed
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/32—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with introduction into the fluidised bed of more than one kind of moving particles
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • B01J2208/00557—Flow controlling the residence time inside the reactor vessel

Definitions

  • the present invention relates to a catalytic cracking process of petroleum hydrocarbons ire the absence of hydrogen
  • U.S. Pat. No. 5,043,522 and U.S. Pat. No. 5,846,403 relate to the improvements of conventional catalytic cracking process, in which part of catalytic gasoline is fed to a riser reactor at upstream of the feedstock nozzles to contact a regenerated catalyst having high activity at a high temperature, so that the yields of light olefins such as propylene, butylene and the like are increased, meanwhile the octane number of gasoline is improved.
  • CN 1279270 A discloses a process for increasing simultaneously yields of both liquefied petroleum gas and diesel oil.
  • a catalytic gasoline is also fed to a riser reactor at upstream of the feedstock nozzles to contact at first and then react with a regenerated catalyst.
  • This part of reprocessed catalytic gasoline is cracked fully at a high temperature under a large catalyst-oil ratio to form a great quantity of liquefied petroleum gas.
  • coke is deposited on the catalyst in a minute quantity, so that the catalyst activity is reduced appropriately in favor of producing more diesel oil,
  • U.S. Pat. No. 3,994,933 discloses a catalytic cracking process with two riser reactors sharing a disengager In this process, a light cycle oil is fed to a riser reactor to contact a regenerated catalyst, resulting in a conversion less than 30%; the spent catalyst is fed to another riser to contact a fresh feedstock and heavy cycle oil.
  • CN 1069054 A discloses a flexible and multi-purpose catalytic cracking process of hydrocarbons. This process relates to two independent riser reactors and two sedimentation separation systems attached with the risers.
  • a light hydrocarbon is contacted and reacted with a regenerated catalyst under conditions of a temperature of 600-700° C., a catalyst-oil ratio of 10-40, a reaction time of 2-20 seconds, and the carbon content of the catalyst being controlled in the range of 0.1-0.4% by weight; the spent catalyst is fed to the other riser to contact heavy hydrocarbons under conventional catalytic cracking reaction conditions.
  • the catalytic conversion processes for treating simultaneously light oil and heavy oil disclosed in the prior art can be essentially divided into two categories: (1) using a single riser reactor and charging the light feedstock to the upstream point of heavy feedstock inlet, and (2) using two riser reactors and treating different feedstocks in different risers.
  • the first category of the processes need a little modification on equipment, however, reaction conditions of light oils are basically fixed, and product distribution and product properties can hardly be improved by means of optimization of operation variables.
  • the second category of the processes overcomes disadvantages of the first category of processes, operation conditions of each riser can be adjusted independently to carry out each reaction under respective conditions adapted to different feedstocks.
  • costs in both construction of unit and reconstruction of equipment are increased significantly.
  • a complicated flowchart will greatly increase the difficulty in operation.
  • An object of the present invention is to provide a catalytic cracking process of petroleum hydrocarbons using a tube-in-tube riser reactor, which can provide hydrocarbon feedstocks having different properties with suitable reaction conditions and improve obviously the product distribution and product properties of the catalytic cracking process.
  • Another object of the present invention is to provide a relay cracking process of petroleum hydrocarbons, which can make the catalytic cracking process not only have a desirable ability to convert heavy oils and better product selectivity but also simplify flowchart and easy to operate.
  • the catalytic cracking process provided in the present invention comprises the following steps
  • reaction stream both from the inner tube and from the annular space between the inner and outer tubes flows together at the inlet of a confluence tube, and then enters a separation apparatus via the confluence tube, where a hydrocarbon product stream is separated from a spent catalyst;
  • Another catalytic cracking process of petroleum hydrocarbons provided in the present invention mainly comprises the following steps:
  • reaction stream from the inner tube and the regenerated catalyst (stream) from the annular space flow together in the confluence tube, and making the reaction stream react continuously under catalytic cracking conditions; introducing the resulting reaction stream to a separation apparatus via the confluence tube, where a hydrocarbon product stream is separated from a spent catalyst;
  • the processes provided in the present invention are simple in equipment and flexible in operation. Not only the reactions of heavy oils and light oils can be carried out separately in their respective reaction zones, but also reaction conditions can be regulated flexibly according to physical-chemical properties and mass flow of different feedstocks, which thus create favorable conditions for improving product distribution and product quality.
  • the processes provided in the present invention can make flexible arrangements of several production schemes such as, for example, gasoline scheme, diesel oil scheme, liquefied petroleum gas scheme, light olefins scheme and the like. Therefore, petroleum refineries can adjust product distribution pattern in time by using the processes of the present invention in accordance with variation of market demand so as to obtain more profitably economic benefit.
  • the processes of the present invention can obviously improve catalytic cracking product distribution, reduce yields of dry Gas and coke, increase yields of high value products such as liquefied petroleum as, gasoline and/or diesel oil and the like.
  • the processes provided in the present invention can also improve the product quality and reduce the environmental pollution caused by petroleum products It is proved by test that the processes can decrease olefin content of gasoline and increase the octane number of gasoline, reduce freezing point of diesel oil., improve sensibility of the diesel oil to flow improvers, increase stability of the diesel oil; meanwhile, the processes have a certain effect in reducing contents of the impurities such as sulfur, nitrogen and the like in gasoline and diesel oils.
  • FIG. 1 is a schematic structure diagram of a tube-in-tube riser reactor having a single conduit for feeding catalyst.
  • FIG. 2 is a schematic structure diagram of joint regions for an inner tube, an outer tube and a confluence tube in a tube-in-tube riser reactor having a single conduit for feeding catalyst.
  • FIG. 3 is a schematic diagram of setting modes of feed nozzles of an inner tube and an outer tube in a tube-in-tube riser reactor having a single conduit for feeding catalyst.
  • FIG. 4 is a schematic structure diagram of a tube-in-tube riser reactor having two conduits for feeding catalyst.
  • FIG. 5 is a schematic structure diagram of joint regions for an inner tube, an outer tube and a confluence tube in a tube-in-tube riser reactor having two conduits for feeding catalyst.
  • FIGS. 6 - 9 are principle flowcharts of the catalytic cracking processes of petroleum hydrocarbons using a tube-in-tube riser reactor
  • FIGS. 10 and 11 are principle flowcharts of the relay cracking process of petroleum hydrocarbons.
  • the tube-in-tube riser reactor is used both in the catalytic cracking process of petroleum hydrocarbons and in the catalytic relay cracking process of petroleum hydrocarbons of the present invention.
  • Said tube-in-tube riser reactor may have a single conduit or two conduits for feeding catalyst, or other reactors having similar structure.
  • the structure of the tube-in-tube riser reactor is illustrated in detail hereinbelow in combination with the Figures
  • said tube-in-tube riser reactor with a single conduit for feeding, catalyst has a structure shown in FIG. 1.
  • the reactor mainly includes the following members, regenerated catalyst inlet conduit 1 , inner tube 2 , outer tube 3 , confluence tube 4 , pre-lifting distribution rings 5 , 6 and 7 , and feed nozzles 8 and 9 ; wherein the inner tube 2 and outer tube 3 are coaxial, and the ratio of the cross-section area of the inner tube to the cross-section area of the annular space between the inner and outer tubes is 1:0.1-10, preferably 1:0.2-2, the lower end of the inner tube 2 is located at a place above the inlet of regenerated catalyst, the inner tube has a length amounting to 10-70% of the total length of the reactor, preferably 20-60%; one end of the confluence tube 4 is connected with the upper end of the outer tube 3 , and the other end is connected with a gas/solid separation apparatus, the cross-section area ratio of the confluence tube 4 and
  • the distance from the upper end of the inner tube (i.e. the outlet end of the inner tube) to the outlet end of the confluence tube is 1-30 meters (i.e., total length of the confluence tube), preferably 2-20 meters.
  • Different types of the joint modes between the inner tube, the outer tube and the confluence tube may be set in accordance with requirements.
  • FIG. 2 exemplifies four embodiments of the joint modes in the present invention, but does not intend to limit the present invention.
  • the upper end of the inner tube is in a straight tube shape, and the outer tube is also in a straight tube shape; both the inner diameters of the confluence tube and the outer tube are the same.
  • the inner tube has an inner diameter of D 1
  • the confluence tube has an inner diameter of D 2
  • D 1 :D 2 0.4-0.9:1.
  • the upper outlet section of the inner tube is diverged in diameter
  • the outer tube is a straight tube
  • both the confluence tube and the outer tube are equal in inner diameters
  • the inner tube has an inner diameter of D 1 and the confluence tube has an inner diameter of D 2 .
  • the ratio of the height H 1 of the upper outlet section of the inner tube to the inner diameter D 1 of the inner tube is 0.5-3:1
  • the divergence angle a of the upper outlet section of the inner tube is 5-3°.
  • the upper outlet section of the inner tube is diverged in diameter, and the outer tube is converged in diameter and then connected with the confluence tube.
  • the inner tube has an inner diameter of D 1 and the confluence tube has an inner diameter of D 2 ,
  • the ratio of the height H 2 of the upper outlet section of the inner tube to the inner diameter D 1 of the inner tube is 0.5-3:1.
  • the divergence angle b of the upper outlet section of the inner rube is 5-30°.
  • the bottom end of the converged section of the outer tube is located between 1.0 D 2 above the inner tube outlet and 1.0 D 2 below the inner tube outlet with the convergence angle c of 10-60°.
  • the ratio of the height H 3 of the converged section of the outer tube to the inner diameter D 2 of the confluence tube is 0.5-3.0:1.
  • the upper end of the inner tube is in a straight tube shape, and the outer tube is converged in diameter and then is connected with the confluence tube.
  • the inner tube has an inner diameter of D 1 and the confluence tube has an inner diameter of D 2 .
  • the bottom end of the converged section of the outer tube is located 10.5 between 1.0 D 2 above the inner tube outlet and 1.0 D 2 below the inner tube outlet with the convergence angle d of 5-45°.
  • the ratio of the height H 4 of the converged section in the outer tube to the inner diameter D 2 of the confluence tube is 0.5-3.0:1.
  • Three kinds of designs for diverged, equal and converged diameters may be used to the lower end of the inner tube in the tube-in-tube riser reactor having a single conduit for feeding catalyst
  • the ratio of the height H 5 of the inlet section at lower part of the inner tube to the inner diameter D 1 of the inner tube is 0.5-3:1 with the divergence angle e of ⁇ 30-30°.
  • Three kinds of designs for diverged, equal and converged diameters may be also used to the lower end of the outer tube, in which the specific design concept is similar to the design of the pre-lifting section in a conventional catalytic cracking riser reactor
  • feed nozzle 8 of the tube-in-tube riser reactor having a single conduit for feeding catalyst may be installed at lower part of the inner tube at a place 5-30% of its total length, also, 2-4 layers of feed nozzles may be set along the inner tube. Or, as shown in FIG. 3, the feed nozzle may be set along central axis of the reactor so that it passes through the lower part of the outer tube and then gets into 0.1-3.0 meters in the inner tube. Feed nozzle 9 may be set at the lower part of the out tube at a place 5-30% of its total length; also, 2-4 layers of feed nozzles may be set in vertical direction of the outer tube.
  • Feed nozzles 8 and 9 may be used in any form favorable to disperse homogeneously hydrocarbon feedstock.
  • Feed nozzles 8 or 9 may consist of 2-12 feed nozzles arranged uniformly along circumferential direction.
  • a quenching media nozzle may be set at the confluence tube in order to create conditions for injecting a quenching media.
  • a relatively flexible feeding mode may be used, and multi-point feed injection may be performed in the inner tube and outer tube.
  • the tube-in-tube riser reactor having two conduits for feeding catalyst has a structure shown in FIG. 4.
  • the reactor mainly includes the following members: catalyst inlet conduits 21 and 22 , inner tube 35 , outer tube 36 , confluence tube 38 , pre-lifting distribution rings 31 and 33 , arid feed nozzles 32 and 34 .
  • inner tube 35 and outer tube 36 are coaxial, and the ratio of cross-section area of the inner tube to cross-section area of the annular space between the inner and outer tubes is 1:0.1-10, preferably 1:0.1-2
  • the catalyst inlet conduit 21 is connected with the lower end of the inner tube 35 , which has a length of 10-70% of total length of the reactor, preferably 15-50%.
  • a distance from the lower end of the outer tube 36 to the lower end of the inner tube 35 is 2-20% of total length of the reactor, preferably 5-15%.
  • the catalyst inlet conduit 22 is connected with the lower end of the outer tube 36 .
  • One end of the confluence tube 38 is connected with the upper end of the outer tube 36 , and the other end is connected with a gas/solid separation apparatus.
  • a cross-section area ratio of the confluence tube 38 to the inner tube 35 is 1:0.2-0.8, preferably 1:0.3-0.7.
  • the pre-lifting distribution rings 31 and 33 are located at the bottom of the inner tube and the bottom of the annular space between the inner and outer tubes respectively.
  • Feed nozzles 32 and 34 are located at the lower parts of the inner tube and the outer tube respectively.
  • Fixing member 30 may be installed in multi-lines, for example, with 2-12 lines of shrouding wires or draw-bars between the inner and outer tubes according to specific size of the reactor and requirements of the engineering.
  • the distance from the upper end of the inner tube (i.e. the outlet end of the inner tube) to the outlet end of the confluence tube (i.e. total length of the confluence tube) is 0 5-20 meters, preferably 1-10 meters. It is desirable to optimize the inner diameter of the confluence tube according to the linear velocity of oil-gas in the confluence tube, and the linear velocity of the oil-gas in the confluence tube should be 0.5-2.0 times of the linear velocity at the inner tube outlet, preferably 0.8-1.2 times.
  • the initial apparent linear velocity of the pre-lifting media is 0.3-8 m/s in the inner tube, and the apparent linear velocity of the pre-lifting media is 0.2-10 m/s in the outer tube.
  • connection regions of the inner tube, the outer tube and the confluence tube may be used with different ways according to requirements.
  • FIG. 5 shows four modes of embodiments, which however do not intend to limit the modes used for the reactor.
  • the upper end of the inner tube is in a straight tube shape
  • the outer tube is also in a straight tube shape
  • the confluence tube and outer tube are equal in inner diameter.
  • the inner tube has an inner diameter of M 1
  • the confluence tube has an inner diameter of M 2
  • M 2 1.5-5:1.
  • the upper outlet sects of the inner tube is diverted in diameter
  • the outer tube is a straight tube
  • the confluence tube and outer tube are equal in inner diameter.
  • the inner tube has an inner diameter of M 1 and the confluence tube has an inner diameter of M 2
  • the ratio of the height N 1 of the upper outlet section of the inner tube to the inner diameter M 1 of the inner tube is 0.5-3. 1 .
  • the divergence angle a 1 of the upper outlet section of the inner tube is 5-30°.
  • the upper outlet section of the inner tube is diverged in diameter, and the outer tube is connected with the confluence tube after converged in diameter.
  • the inner tube has an inner diameter of M 1 and the confluence tube has an inner diameter of M 2 .
  • the ratio of the height N 2 of the upper outlet section of the inner tube to the inner diameter M 1 of the inner tube is 0.5-3:1.
  • the divergence angle b 1 of the upper outlet section of the inner tube is 5-30°.
  • the bottom end of the converged section in the outer tube is located between 1.0 M 2 above the inner tube outlet and 1.0 M 2 below the inner tube outlet with the convergence angle c 1 of 10-60°.
  • the ratio of the height N 3 of the converged section of the outer tube to the inner diameter M 2 of the confluence tube is 0.5-3.0:1.
  • the upper end of the inner tube is in a straight tube shape, and the outer tube is connected with the confluence tube after converged in diameter.
  • the inner tube has an inner diameter as M 1 and the confluence tube has an inner diameter as M 2
  • the bottom end of the converged section of the outer tube is located between 1.0 M 2 above the inner tube outlet and 1.0 M 2 below the inner tube outlet with the convergence angle d 1 of 5-45°.
  • the ratio of the height N 4 of the converged section, in the outer tube to the inner diameter M 2 of the confluence tube is 0.5-3.0:1.
  • the design of both lower ends of the inner tube and the outer tube in the tube-in-tube riser reactor having two conduits for feeding catalyst is basically similar to that of the pre-lifting section in a conventional catalytic cracking riser reactor.
  • the design of the pre-lifting distribution rings 31 and 33 are also basically similar to that in a conventional catalytic cracking process.
  • the feed nozzle 32 is set at a position of 5-30% of total inner tube length along the lower part of the inner tube
  • Feed nozzle 34 is set at a position of 5-30% of the total outer tube length along the lower part of the outer tube.
  • Feed nozzles 32 and 34 may be used in any form, provided that it is favorable to disperse hydrocarbon feedstock homogeneously. Both feed nozzles 32 and 34 may consist of 2-12 feed nozzles, and said nozzles should be arranged uniformly along circumferential direction.
  • the catalysts fed via catalyst inlet conduit respectively to the inner tube and the annular space between the inner and outer tubes of the tube-in-tube riser reactor may be the same or different.
  • the catalysts fed to the inner tube and the annular space between the inner and outer tubes of the tube-in-tube riser reactor may be the regenerated catalysts from a regenerator at high temperature.
  • the catalysts may be a mixture of the regenerated catalyst and a spent catalyst and/or a semi-regenerated catalyst
  • the regenerated catalyst may be fed to the inner tube of the tube-in-tube riser reactor, and the semi-regenerated catalyst or spent catalyst or a mixture thereof may be fed to the annular space between the inner tube and outer tube, and vice versa.
  • the catalyst fed to the catalyst inlet conduit may be contemplated comprehensively and rearranged flexibly in accordance with the unit conditions, feedstock properties and requirement for the desired products.
  • the catalysts to be fed to the tube-in-tube riser reactor may also be cooled via a catalyst cooler, or may be fed to the tube-in-tube riser reactor via catalyst inlet conduit after the regenerated catalyst and spent catalyst and/or semi-regenerated catalyst are fully mixed in a catalyst blending vessel.
  • the catalysts used in the present invention may be any catalyst suitable for catalytic cracking process, of which active components are at least one kind of zeolite selected from a group consisting of Y-type or HY-type zeolite containing or not containing rare earth and/or phosphorous, ultra-stable Y-type zeolite containing or not containing rare earth and/or phosphorous, ZSM-5 family zeolite or high-silica zeolite having a pentasil structure, ⁇ -zeolite, ferrierite, and also an amorphous alumina-silica catalyst.
  • the inner tube and the annular space between the inner and outer tubes may use two different kinds of catalysts.
  • the bottom of the tube-in-tube riser reactor, the bottom of the inner tube and the bottom of the annular space between the inner and outer tubes are furnished with an inlet of a pre-lifting media respectively.
  • Steam, dry gas or a mixture thereof can be used as a pre-lifting media.
  • the apparent linear velocity of the pre-lifting gas in the inner tube is initially 0.3-6.0 m/s, and the apparent linear velocity of the pre-lifting gas in the annular space between the inner and outer tubes is 0.2-8.0 m/s.
  • the hydrocarbon feedstocks fed to the inner tube and the annular space between the inner and outer tubes may be selected from a group consisting of: gaseous hydrocarbon, refinery gas, primary processing gasoline fraction, secondary processing gasoline fraction, primary processing diesel oil fraction, secondary processing diesel oil fraction, straight run gas oil, coker gas oil, deasphalted oil, hydrofined oil, hydrocracking tail oil, vacuum residuum and a mixture thereof.
  • the hydrocarbon feedstock fed to the inner tube is preferably selected from a group consisting of straight run gas oil, coker gas oil, deasphalted oil, hydrofined oil, hydrocracking tail oil, vacuum residuum, atmospheric residuum and a mixture thereof.
  • the hydrocarbon feedstock fed to the annular space between the inner and outer tubes is preferably selected from a group consisting of gaseous hydrocarbon, refinery gas, primary processing gasoline fraction, secondary processing gasoline fraction, primary processing diesel oil fraction, secondary processing diesel oil fraction and a mixture thereof.
  • the reaction conditions of the hydrocarbon feedstock in the inner tube are as follows a reaction temperature of 460-580° C.; preferably 480-550° C., a reaction pressure of 0.1-0 6 MPa, preferably 0.2-0.4 MPa; a catalyst-oil ratio (weight ratio of catalyst to feedstock) of 3-15, preferably 4-10; an oil-gas residence time of 1.0-10 seconds in the inner tube, preferably 1.5-5.0 seconds, a catalyst temperature of 620-720° C. before contacting the hydrocarbon feedstock, preferably 650-700° C.; and an atomization steam amount of 1-20% by weight (based on the hydrocarbon feedstock), preferably 2-15% by weight.
  • Reaction conditions of the hydrocarbon feedstock in the annular space between the inner and outer tubes are as follows: a reaction temperature of 300-680° C., preferably 400-600° C., a reaction pressure of 0.1-0.6 MPa, preferably 0.2-0.4 MPa; a catalyst-oil ratio of 2-30, preferably 4-20, an oil-as residence time of 0.5-20 seconds, preferably 1-15 seconds; and an atomization steam amount of 1-20% by weight (based on the hydrocarbon feedstock), preferably 1-15% by weight.
  • the reaction conditions of the hydrocarbon feedstock in the annular space between the inner and outer tubes can be further optimized in the light of the properties of the hydrocarbon feedstock and the requirement of the desired product.
  • reaction temperature a reaction temperature of 530-680° C., a catalyst-oil ratio of 8-30, an oil-gas residence time of 5-20 seconds and the like.
  • relatively moderate operation conditions should be adopted, for example, a reaction temperature 300-540° C., a catalyst-oil ratio of 2-9, an oil-gas residence time of 1-5 seconds, and the like.
  • reaction stream both in the inner tube and in the annular space between the inner and outer tubes is mixed at the inlet of the confluence, and then continues to react in the confluence tube, wherein the reaction time is 0.1-3.0 seconds, and the reaction pressure, temperature, catalyst-oil ratio and the like depend on the reaction conditions in the inner tube and the annular space.
  • reaction temperature is 450-600° C.
  • catalyst-oil ratio is 4-12
  • reaction pressure is 0.1-0.6 MPa
  • weight ratio of steam to the hydrocarbon feedstock is 0.01-0.15:1.
  • the catalyst is fed to the bottom of the tube-in-tube riser reactor having single conduit for feeding catalyst via a catalyst inlet conduit 1 , and flows upwards under an action of a pre-lifting media.
  • a part of the catalyst (for example, 20-80 wt. % of the catalyst) flows into the inner tube 2 and the remaining part of the catalyst enters the annular space between the inner tube 2 and outer tube 3 , both of them continue to flow upwards under the action of the pre-lifting media.
  • the hydrocarbon feedstocks are fed via nozzles 8 and 9 to the inner tube and the annular space between the inner and outer tubes respectively to contact the catalyst, and both the reaction streams continue to flow upward along vessel wall.
  • reaction streams both from the inner tube and from the annular space between the inner and outer tubes flow together at the inlet of the confluence tube 4 , then the mixed stream enters to the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus, where a hydrocarbon product stream is separated from a spent catalyst; then the separated hydrocarbon product stream enters the subsequent separation system 14 to be separated further into different products.
  • the spent catalyst falls down into the stripper 13 , where the reaction oil-gas entrained by the catalyst is stripped off by the action of steam; the stripped catalyst is introduced to the regenerator 15 to burn off coke with air. The regenerated catalyst is recycled to the reactor for reuse.
  • the catalyst is fed to the bottom of the tube-in-tube riser reactor having single conduit for feeding catalyst via the catalyst inlet conduit 1 , and flows upward under the action of a pre-lifting media.
  • a part of the catalyst (for example, 20-80 wt. % of the catalyst) flows into the inner tube 2 , and the remaining part of the catalyst enters the annular space between the inner tube 2 and outer tube 3 , both of them continue to flow upwards under the action of the pre-lifting media.
  • the hydrocarbon feedstocks are fed via nozzles 8 and 9 into the inner tube and the annular space between the inner and outer tubes of the reactor respectively to contact the catalyst, and the reaction streams flow upwards continuously along vessel wall.
  • the reaction streams both from the inner tube and from the annular space between the inner and outer tubes flow together at the inlet of the confluence tube 4 , and the mixed stream enters the disengager 12 via the confluence tube and a gas/solid rapid separation apparatus, where a hydrocarbon product stream is separated from a spent catalyst.
  • the separated hydrocarbon product stream enters the subsequent separation system 14 to be further separated into various products, and the spent catalyst falls down into the stripper 13 where the reaction oil-gas entrained by the catalyst is stripped off under the action of steam.
  • the stripped catalyst is fed to the regenerator 15 to burn off coke with air, and then the regenerated catalyst is introduced to the blending vessel 16 to mix with the spent catalyst and/or semi-regenerated catalyst.
  • the mixed catalyst is recycled to the reactor for reuse.
  • the regenerated catalyst is fed via catalyst inlet conduits 21 and 22 to the inner tube 35 and the annular space between the inner tube 35 and outer tube 36 in the tube-in-tube riser reactor having two conduits for feeding catalyst respectively, and flows upward under the action of pre-lifting media.
  • the hydrocarbon feedstock is fed via nozzles 32 and 34 to the inner tube and the annular space between the inner and outer tubes respectively to contact the catalyst, and the reaction stream flows upward along vessel wall.
  • the reaction streams both from the inner tube and from the annular space between the inner and outer tubes flow together at the inlet of the confluence tube 38 , and the mixed stream enters the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus.
  • a hydrocarbon product stream is separated from a spent catalyst.
  • the separated hydrocarbon product stream enters the subsequent separation system 14 to be further separated into various products
  • the spent catalyst falls down into the stripper 13 where the reaction oil-gas entrained by the catalyst is stripped off under the action of steam,
  • the stripped catalyst is fed to the regenerator 15 to burn coke off with air, and then the regenerated catalyst is recycled into the reactor for reuse.
  • the regenerated catalyst is fed to the bottom of the inner tube 35 via catalyst inlet conduit 21 in the tube-in-tube riser reactor and flows upward under the action of a pre-lifting media
  • a part of spent catalyst flows via the catalyst inlet conduit 22 into the annular space between the inner tube 35 and outer tube 36 and flows upward under the action of the pre-lifting media.
  • the hydrocarbon feedstock is fed via nozzles 32 and 34 to the inner tube and the annular space between the inner and outer tubes respectively to contact the catalyst, and the reaction streams flow upward along vessel wall.
  • Reaction streams both from the inner tube and from the annular space between the inner and outer tubes flow together at the inlet of the confluence tube 38 , and the mixed stream enters the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus.
  • a hydrocarbon product stream is separated from a spent catalyst.
  • the separated hydrocarbon product stream enters the subsequent separation system 14 to be further separated into various products, and the spent catalyst falls down into the stripper 13 where the reaction oil-gas entrained by catalyst is stripped off under the action of steam.
  • the stripped spent catalyst is fed partially to the regenerator 15 to burn coke off with air, and the regenerated catalyst is recycled to the bottom of the inner tube for reuse The remaining part of the spent catalyst is recycled directly to the bottom of the annular space between the inner and outer tubes for reuse without regeneration.
  • the regenerated catalyst, spent catalyst and semi-regenerated catalyst, or a mixture of any two thereof to be fed to the reactor can be fed via the catalyst inlet conduit to the bottom of the tube-in-tube riser reactor after being cooled via a catalyst cooler.
  • the reactor, catalyst, feedstock and operation conditions used in the relay cracking process of petroleum hydrocarbons provided in the present invention are substantially similar to those in the catalytic cracking process of petroleum hydrocarbons using tube-in-tube riser reactor aforementioned. The difference between them lies in that, the hydrocarbon feedstock is fed only to the inner tube of the tube-in-tube riser reactor but not to the annular space between the inner tube and outer tube.
  • the relay cracking process of petroleum hydrocarbons is different from the catalytic cracking process of petroleum hydrocarbon using tube-in-tube riser reactor aforementioned in the aspects of feedstock and operation conditions.
  • the hydrocarbon feedstock fed into the inner tube is selected from a group consisting of gaseous hydrocarbon, refinery gas, primary processing gasoline fraction, secondary processing gasoline fraction, primary processing diesel oil fraction, secondary processing diesel oil fraction, straight run gas oil, coker gas oil, deasphalted oil, hydrofined oil, hydrocracking tail oil, vacuum gas oil, vacuum residuum, atmospheric residuum and a mixture thereof.
  • gaseous hydrocarbon refinery gas
  • primary processing gasoline fraction secondary processing gasoline fraction
  • primary processing diesel oil fraction primary processing diesel oil fraction
  • secondary processing diesel oil fraction straight run gas oil
  • coker gas oil deasphalted oil
  • hydrofined oil hydrocracking tail oil
  • vacuum gas oil vacuum residuum
  • atmospheric residuum atmospheric residuum and a mixture thereof.
  • the reaction of the hydrocarbon feedstock in the inner tube is carried out under conditions as follows a reaction temperature of 480-700° C., preferably 500-680° C.; a reaction pressure of 0.1-0.6 MPa, preferably 0.2-0.4 MPa; a catalyst-oil ratio of 3-30, preferably 4-25; an oil-gas residence time of 1.0-10 seconds in the inner tube, preferably 1.5-5.0 seconds; a catalyst temperature of 620-800° C. before contacting hydrocarbon feedstock, preferably 640-750° C. and an atomization steam amount of 1-45% by weight (based on feedstock), preferably 2-35% by weight.
  • Reaction conditions of the hydrocarbons in the confluence tube are as follows: a reaction temperature of 490-720° C., preferably 500-700° C.; a reaction pressure of 0.1-0.6 MPa, preferably 0.2-0.4 MPa; a catalyst-oil ratio of 4-40, preferably 5-30; an oil-gas residence time of 0.5-10 seconds in the confluence tube, preferably 1.0-5.0 seconds; and a steam-oil ratio of 3-45% by weight, preferably 5-35% by weight.
  • the steam-oil ratio means the weight ratio of steam to hydrocarbon feedstock.
  • the regenerated catalyst is fed via the catalyst inlet conduit 1 to the bottom of the tube-in-tube riser reactor having single conduit for feeding catalyst, and flows upward under the action of a pre-lifting media; 20-80% by weight of catalyst flows into the inner tube 2 , the remaining part of catalyst enters the annular space between the inner tube 2 and outer tube 3 , and both the parts of the catalyst continue to flow upward under the action of the pre-lifting media.
  • the hydrocarbon feedstock is fed to the inner tube of the reactor via nozzle 8 to contact the catalyst. And the reaction stream flows upward continuously along vessel wall.
  • the reaction stream from the inner tube flows together at the inlet of the confluence tube 4 with the regenerated catalyst (stream) from the annular space between the inner and outer tubes, and then the mixed reaction stream enters the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus, where a hydrocarbon product stream is separated from a spent catalyst.
  • the separated hydrocarbon product stream enters the subsequent separation system 14 to be further separated into various products, and the spent catalyst falls down into the stripper 13 where the reaction oil-gas entrained by catalyst is striped off under the action of steam.
  • the stripped catalyst is fed to the regenerator 15 to burn off coke with air, and the regenerated catalyst is recycled to the reactor for reuse.
  • the regenerated catalyst is fed via the catalyst inlet conduits 21 and 22 to the inner tube 35 and the annular space between the inner tube 35 arid outer tube 36 of the tube-in-tube riser reactor having two conduits for feeding catalyst respectively, and flows upward under the action of a pre-lifting media
  • the hydrocarbon feedstock is fed to the inner tube of the reactor via the nozzle 32 to contact the catalyst, and the reaction stream flows upward along vessel wall
  • the reaction stream from the inner tube flows together at the inlet of the confluence tube 38 with the regenerated catalyst (stream) from the annular space between the inner tube 35 and outer tube 36
  • the mixed stream enters the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus In the disengager, the hydrocarbon product stream and the spent catalyst are separated.
  • the separated hydrocarbon product stream enters the subsequent separation system 14 to be further separated into various products.
  • the spent catalyst falls down into the stripper 13 where the reaction oil-gas entrained by catalyst is stripped off under the action of steam.
  • the stripped catalyst is introduced to the regenerator 15 to burn off coke with air, and the regenerated catalyst is recycled to the reactor for reuse.
  • the regenerated catalyst to be fed to the reactor can be fed to the bottom of the tube-in-tube riser reactor after being cooled via a catalyst cooler.
  • the catalyst used in the Examples is a commercial product from Catalyst Factory, Lan Zhou Petrochemical Corp., Trademark LV-23, of which major properties are shown in Table 1.
  • the hydrocarbon feedstock used in the Examples is DaQing VGO blended with 30% by weight of VR, of which properties are shown in Table 2.
  • the testing apparatus used in the Examples is a pilot FCC unit adopted tube-in-tube riser reactor.
  • the present example shows test results obtained by using the process provided in the present invention when light oil is produced as main object product.
  • the hydrocarbon product stream was separated from the spent catalyst, and then entered a subsequent fractionation system via an oil-gas pipeline to be further fractionated into various products.
  • the products were metered and analyzed respectively.
  • Spent catalyst was stripped with steam, then introduced into a regenerator to burn off coke with air. The regenerated catalyst was recycled to the reactor for reuse.
  • the present example shows test results obtained by using the process provided in the present invention when a liquefied petroleum gas is produced as main object product.
  • the hydrocarbon product stream was separated from the spent catalyst, then entered a subsequent fractionation system via an oil-gas pipeline to be further fractionated into various products
  • the products were metered and analyzed respectively.
  • the spent Do catalyst was stripped with steam, and then introduced to a regenerator to burn off coke with air. The regenerated catalyst was recycled to the reactor for reuse.
  • the main operation conditions are shown in Table 3, the product distribution is shown in Table 4, and the main product properties are shown in Table 5 It can be seen from Tables 4 and 5 that when liquefied petroleum gas is produced as main object product, the yield of liquefied petroleum gas can amount to 29.46% by weight and the total yield of liquid products can amount to 86.65% by weight with a lower yield of dry gas and coke.
  • the present example shows test results obtained by using the process provided in the present invention when gasoline is produced as main object product.
  • the main steps of the test are as follows.
  • the feedstock shown in Table 1 and the recycled oil produced in the present unit were mixed, then the mixed oil was heated via a preheating furnace and fed to the inner tube of the tube-in-tube riser reactor to contact the regenerated catalyst flowing from the regenerator and lifted with a pre-lifting media.
  • Both the reaction stream in the inner tube and the reaction stream in the annular space moved up along vessel wall respectively, mixed with each other in the confluence tube to continue the reaction, and then entered a disengager.
  • the hydrocarbon product stream was separated from the spent catalyst, and then entered a subsequent fractionation system via an oil-gas pipeline to be further fractionated into various products The products were metered and analyzed respectively.
  • the spent catalyst was stripped with steam, then introduced to a regenerator to burn off coke with air. The regenerated catalyst was recycled to the reactor for reuse.
  • the present example shows test results obtained by using the process provided in the present invention when diesel oil is produced as main object product.
  • Both the reaction stream in the inner tube and the reaction stream in the annular space moved up along vessel wall respectively, then mixed with each other in the confluence tube to continue the reaction, and then entered a disengager
  • the hydrocarbon product stream was separated from the spent catalyst, and then entered a subsequent fractionation system via an oil-gas pipeline to be further fractionated into various products.
  • the products were metered and analyzed respectively.
  • the spent catalyst was stripped with steam, then part of the stripped catalyst was introduced into a regenerator to burn off coke with air, and the remaining part of the spent catalyst was fed directly into the catalyst blending vessel 16 to mix with the regenerated catalyst in a blending ratio of the regenerated catalyst to the spent catalyst of 2:1. Then the mixed catalyst was recycled to the reactor for reuse.
  • the present example shows test results obtained by using the process provided in the present invention when liquefied petroleum gas and diesel oil are produced as main object products.
  • the main steps of test are as follows.
  • the feedstock shown in Table 1 was mixed with the recycled oil from the present unit, and the mixed oil was heated via a preheating furnace and then fed to the inner tube of the tube-in-tube riser reactor to contact the regenerated catalyst flowing from regenerator and lifted with a pre-lifting media.
  • the gasoline fraction produced in the present unit was fed to the annular space between the inner and outer tubes to contact the regenerated catalyst therein. Both the reaction stream in the inner tube and the reaction stream in the annular space moved up along vessel wall respectively, mixed each other in the confluence tube to continue the reaction, and then entered a disengager.
  • the hydrocarbon product stream was separated from the spent catalyst, and entered a subsequent fractionation system via an oil-gas pipeline to be further fractionated into various products.
  • the products were metered and analyzed respectively.
  • the spent catalyst was stripped with steam, and then introduced to a regenerator to burn off coke with air. The regenerated catalyst was recycled to the reactor for reuse.
  • the relay cracking process will be further illustrated but not limited.
  • the catalysts used in the examples below were commercial products with trademarks respectively of RMG, CIP-1 and CFP manufactured by China's QiLu Petrochemical Catalyst Factory, and the three kinds of catalysts were hydrothermally aged, of which the main properties are shown in Table 6.
  • the hydrocarbon feedstock used is DaQing VGO blended with 30% by weight of VR, of which properties are shown in Table 1, and the testing apparatus used in the Examples below was a pilot FCC unit adopted tube-in-tube riser reactor.
  • the present example illustrates that higher yields of liquefied petroleum gas, gasoline and diesel oil can be obtained by using the relay cracking process provided in the present invention with heavy petroleum hydrocarbon as feedstock.
  • the steps of test are mainly as follows. As shown in FIG. 10, the regenerated catalyst was introduced into the bottom of the tube-in-tube riser reactor via the catalyst inlet conduit 1 , and flew upward under the action of a pre-lifting vapor with 70% by weight of the catalyst flew into the inner tube 2 and the remaining 30% by weight of catalyst entered into the annular space between the inner tube 2 and outer tube 3 to continue flowing upward under the action of pre-lifting vapor.
  • the hydrocarbon feedstock as shown in Table 1 was preheated, and fed to the inner tube via the nozzles 8 to contact the catalyst; the reaction stream flew upward continuously along vessel wall.
  • the mixture of the reaction oil-gas and catalyst from the inner tube flew together in the confluence tube 4 with the regenerated catalyst stream from the annular space between the inner tube 2 and outer tube 3 , and the mixed stream flew through the confluence tube and a rapid gas/solid separation apparatus into the disengager 12 , where the hydrocarbon product stream was separated from the spent catalyst.
  • the separated hydrocarbon product stream entered the subsequent separation system 14 to be further separated into various products.
  • the regenerated catalyst was recycled to the reactor for reuse.
  • the present example illustrates that a higher yield of light olefins such as propylene and the like can be obtained by using the relay cracking process of the present invention when a heavy petroleum hydrocarbon is used as feedstock.
  • the reaction stream from the inner tube flew together in the confluence tube 38 with the regenerated catalyst stream from the annular space between the inner tube 35 and the outer tube 36 , and then the mixed stream entered the disengager 12 via a confluence tube and a rapid gas/solid separation apparatus.
  • a hydrocarbon product stream is separated from a spent catalyst.
  • the separated hydrocarbon product stream entered the subsequent separation system 14 to be further separated into various products.
  • the spent catalyst fell down into the stripper 13 where the reaction oil-gas entrained by catalyst was stripped off under the action of steam.
  • the stripped catalyst was introduced to the regenerator 15 to burn coke off with air.
  • the regenerated catalyst was recycled to the reactor for reuse.
  • This example illustrates that higher yield of light olefins such as ethylene and the like can be obtained by using the relay cracking process of the present invention with a heavy petroleum hydrocarbon as feedstock.
  • the hydrocarbon feedstock was fed to the inner tube of the reactor via the nozzle 32 to contact the catalyst, and the reaction stream flew upward along vessel wall
  • the reaction stream from the inner tube flew together at the confluence tube inlet 38 with the regenerated catalyst stream from the annular space between the inner tube 35 and the outer tube 36 , and then entered the disengager 12 via the confluence tube and a rapid gas/solid separation apparatus.
  • the hydrocarbon product stream was separated from the spent catalyst.
  • the separated hydrocarbon product stream flew into the subsequent separation system 14 to be further separated into various products.
  • the spent catalyst fell down into the stripper 13 where the reaction oil-gas entrained by catalyst was stripped off under the action of steam.
  • the stripped catalyst was introduced to the regenerator 15 to burn coke off with air.
  • the regenerated catalyst was recycled to the reactor for reuse.

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CN 01258820 CN2498160Y (zh) 2001-08-29 2001-08-29 一种套管式催化裂化反应器
CN01258820.2 2001-08-29
CN01141477.4 2001-09-27
CN01264042.5 2001-09-27
CN 01264042 CN2506644Y (zh) 2001-09-27 2001-09-27 一种双路进剂套管式催化裂化反应器
CNB011414774A CN1184283C (zh) 2001-09-27 2001-09-27 一种采用套管式反应器的催化裂化方法
CN01134268.4 2001-10-30
CN01134269.2 2001-10-30
CNB011342692A CN1184282C (zh) 2001-10-30 2001-10-30 一种石油烃接力催化裂化方法
CNB011342684A CN1184281C (zh) 2001-10-30 2001-10-30 一种采用双路进剂套管式反应器的催化裂化方法

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US20100051444A1 (en) * 2005-12-16 2010-03-04 Zaikin Yuriy A Self-sustaining cracking of hydrocarbons
US20100163455A1 (en) * 2007-04-13 2010-07-01 Hadjigeorge George A Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
US20100200460A1 (en) * 2007-04-30 2010-08-12 Shell Oil Company Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
US20100324232A1 (en) * 2007-10-10 2010-12-23 Weijian Mo Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
US20110139679A1 (en) * 2009-12-14 2011-06-16 Total Raffinage Marketing Method for catalytic cracking with maximization of diesel base stocks
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US8747759B2 (en) 2011-12-12 2014-06-10 Uop Llc Process and apparatus for mixing two streams of catalyst
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US8815166B2 (en) 2012-03-20 2014-08-26 Uop Llc Process and apparatus for mixing two streams of catalyst
US8916099B2 (en) 2012-03-20 2014-12-23 Uop Llc Process and apparatus for mixing two streams of catalyst
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US9278893B2 (en) 2012-11-12 2016-03-08 Uop Llc Process for making gasoline by oligomerization
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US8764971B2 (en) * 2009-12-14 2014-07-01 Total Raffinage Marketing Method for catalytic cracking with maximization of diesel base stocks
US9181146B2 (en) 2010-12-10 2015-11-10 Exxonmobil Chemical Patents Inc. Process for the production of xylenes and light olefins
US8747657B2 (en) 2011-12-12 2014-06-10 Uop Llc Process and apparatus for mixing two streams of catalyst
US8815082B2 (en) 2011-12-12 2014-08-26 Uop Llc Process and apparatus for mixing two streams of catalyst
US8747758B2 (en) 2011-12-12 2014-06-10 Uop Llc Process and apparatus for mixing two streams of catalyst
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US8747759B2 (en) 2011-12-12 2014-06-10 Uop Llc Process and apparatus for mixing two streams of catalyst
WO2013089875A1 (en) * 2011-12-12 2013-06-20 Uop Llc Process and apparatus for mixing two streams of catalyst
WO2013089876A1 (en) * 2011-12-12 2013-06-20 Uop Llc Process and apparatus for mixing two streams of catalyst
RU2575934C1 (ru) * 2011-12-12 2016-02-27 Юоп Ллк Способ и устройство для смешения двух потоков катализатора
US8815166B2 (en) 2012-03-20 2014-08-26 Uop Llc Process and apparatus for mixing two streams of catalyst
US8916099B2 (en) 2012-03-20 2014-12-23 Uop Llc Process and apparatus for mixing two streams of catalyst
US9375695B2 (en) 2012-03-20 2016-06-28 Uop Llc Process and apparatus for mixing two streams of catalyst
US8936758B2 (en) 2012-03-20 2015-01-20 Uop Llc Process and apparatus for mixing two streams of catalyst
US8921633B2 (en) 2012-05-07 2014-12-30 Exxonmobil Chemical Patents Inc. Process for the production of xylenes and light olefins
US8937205B2 (en) 2012-05-07 2015-01-20 Exxonmobil Chemical Patents Inc. Process for the production of xylenes
US9181147B2 (en) 2012-05-07 2015-11-10 Exxonmobil Chemical Patents Inc. Process for the production of xylenes and light olefins
US9522375B2 (en) 2012-11-12 2016-12-20 Uop Llc Apparatus for fluid catalytic cracking oligomerate
US9567267B2 (en) 2012-11-12 2017-02-14 Uop Llc Process for oligomerizing light olefins including pentenes
US9278893B2 (en) 2012-11-12 2016-03-08 Uop Llc Process for making gasoline by oligomerization
US9434891B2 (en) 2012-11-12 2016-09-06 Uop Llc Apparatus for recovering oligomerate
US9441173B2 (en) 2012-11-12 2016-09-13 Uop Llc Process for making diesel by oligomerization
US9522373B2 (en) 2012-11-12 2016-12-20 Uop Llc Apparatus for oligomerizing light olefins
US10508064B2 (en) 2012-11-12 2019-12-17 Uop Llc Process for oligomerizing gasoline without further upgrading
US9914673B2 (en) 2012-11-12 2018-03-13 Uop Llc Process for oligomerizing light olefins
US9644159B2 (en) 2012-11-12 2017-05-09 Uop Llc Composition of oligomerate
US9663415B2 (en) 2012-11-12 2017-05-30 Uop Llc Process for making diesel by oligomerization of gasoline
US9834492B2 (en) 2012-11-12 2017-12-05 Uop Llc Process for fluid catalytic cracking oligomerate
US9376633B2 (en) 2014-03-31 2016-06-28 Uop Llc Process and apparatus for distributing fluidizing gas to an FCC riser
US9205394B2 (en) 2014-03-31 2015-12-08 Uop Llc Process and apparatus for distributing fluidizing gas to an FCC riser
US20220081624A1 (en) * 2020-09-14 2022-03-17 Saudi Arabian Oil Company Methods for upgrading hydrocarbon feeds to produce olefins

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