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WO2012171426A1 - 一种催化裂化方法及装置 - Google Patents

一种催化裂化方法及装置 Download PDF

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Publication number
WO2012171426A1
WO2012171426A1 PCT/CN2012/075635 CN2012075635W WO2012171426A1 WO 2012171426 A1 WO2012171426 A1 WO 2012171426A1 CN 2012075635 W CN2012075635 W CN 2012075635W WO 2012171426 A1 WO2012171426 A1 WO 2012171426A1
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Prior art keywords
catalyst
zone
oil
gas
reaction
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PCT/CN2012/075635
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English (en)
French (fr)
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石宝珍
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Individual
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Individual
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Priority to US14/126,250 priority Critical patent/US9353316B2/en
Priority to RU2014101022/04A priority patent/RU2554875C9/ru
Publication of WO2012171426A1 publication Critical patent/WO2012171426A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • 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
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4093—Catalyst stripping
    • 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
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/04—Diesel oil

Definitions

  • the invention relates to a catalytic cracking method and device, in particular to a method and a device for catalytic cracking of petroleum hydrocarbon raw materials, belonging to the technical field of petrochemical industry. Background technique
  • Catalytic cracking units are the most important gasoline production units. Most of the world's motor gasoline comes from catalytic cracking units, and conventional catalytic cracking uses riser reactors.
  • the biggest drawback of the existing riser reactor is that the riser is too long, and the catalyst activity at the outlet of the riser is only about 1/3 of the initial activity. Therefore, in the latter half of the riser reactor, the activity and selectivity of the catalyst are sharp. Decrease, poor catalytic activity, thermal cracking reaction and other unfavorable secondary reactions increase not only the single-pass conversion rate, but also the catalytic gasoline olefin content of up to 45%, which is far from meeting the new standard requirements for gasoline. As the activity of the catalyst decreases, the selectivity of the catalytic reaction inevitably decreases, and the side reaction naturally increases.
  • Chinese Patent Application No. 99213769.1 discloses a two-stage tandem device for catalytic cracking, which consists of two structures. The same catalytic cracking unit is formed by overlapping the top and bottom ends. This technology enhances the catalytic activity and selectivity of the conventional riser by shortening the reaction time by using a reaction and regeneration device that overlaps above and below. .
  • the technology disclosed in this patent application is limited to the principle, and lacks an operational implementation method. When the project is implemented, it is equivalent to constructing two sets of catalytic cracking reaction regeneration devices that overlap each other, and the investment cost is high, and the implementation possibility is small.
  • Chinese Patent Application No. 0 012 2845.5 discloses a two-stage catalytic cracking process for a hydrocarbon oil, in which a hydrocarbon oil is first contacted and reacted with a cracking catalyst in a first reactor, and the generated oil and gas is fed into a second reactor and contains a five-membered ring.
  • the catalyst of the high silica zeolite is contacted and reacted, and the generated oil and gas is sent to a fractionation column for separation.
  • the catalyst in the two reactors is a catalyst having different compositions and properties.
  • Chinese Patent Application No. 00134054.9 discloses a new technology for two-stage riser catalytic cracking, which divides the riser into two sections, the first zone catalyst comes from the regenerator, the first zone ends, and the catalyst and oil and gas pass through the end of the first zone.
  • the intermediate splitter is separated, and only the oil and gas continues to enter the second reaction zone reaction; the catalyst of the second reaction zone is a regenerated catalyst from the regenerator that takes heat through the external heat extractor.
  • the technique is in the second stage of the reaction (ie the second half of the riser)
  • the high activity of the cooled low temperature regenerated catalyst is continuously contacted with the oil and gas to increase the activity of the second stage catalyst and increase the single pass conversion.
  • the catalyst separated in the first zone of the technology must be stripped before entering the regenerator, and the regenerated catalyst must be transported upward by the transport medium to enter the second section.
  • the stripping steam and the transport medium will all enter the second section riser. , will inevitably affect the reaction of the second stage; if the amount of stripping steam is limited, it will affect the stripping effect, which will affect the regeneration process; in addition, the height difference from the bottom of the external heat extractor to the inlet of the second reaction section is several tens of meters.
  • the amount of transport medium is large and requires a lot of energy consumption; and the technology requires two settlers, two stripping sections, and the investment is greatly increased. Summary of the invention
  • an object of the present invention is to provide a novel catalytic cracking method which can improve product distribution and product quality, and can reduce engineering investment and facilitate engineering implementation.
  • the present invention first provides a catalytic cracking reaction which is carried out in a reaction portion provided with a riser reactor and a reverse-removal device including a regeneration portion of the regenerator, wherein:
  • the reaction part is composed of a riser reactor, a catalyst stripping zone and a settler;
  • the riser reactor comprises a bottom up pre-lift section, a feedstock oil reaction zone, a catalyst split zone, and a catalyst supplementation zone.
  • a hydrocarbon re-reaction zone the catalyst splitting zone is disposed at an outlet of the feedstock oil reaction zone;
  • a channel is disposed between the catalyst split zone and the oil and gas re-reaction zone, and the periphery of the channel is a supplemental distribution zone of the catalyst;
  • the regenerator is provided with a lower first regeneration zone, a middle dense fluidized bed zone and an upper dilute phase catalyst sedimentation separation zone from bottom to top; the first regeneration zone and the middle dense phase fluidized bed Separate zones can be separated by partitions (eg partitions with channels);
  • the regenerated catalyst from the dense phase fluidized bed zone in the middle of the regenerator enters the pre-lift section and the catalyst replenishment zone of the riser reactor, respectively, in the following manner:
  • the regenerated catalyst directly enters the pre-lift section by gravity (the pre-lift section is located below the nozzle of the feedstock reaction zone of the riser reactor), or the regenerated catalyst is cooled first (the regenerated catalyst can be subjected to gravity) Enter the catalyst temperature controller or cooler to cool down) and then enter the pre-lift section by gravity (can enter by gravity), or regenerate the catalyst and regenerate the catalyst after cooling into the pre-lift section at the same time (depending on gravity) Go down);
  • the regenerated catalyst is cooled into the catalyst (the temperature can be reduced by the regenerative catalyst entering the catalyst temperature controller), and then enters the catalyst supplemental distribution zone by gravity (the regenerated catalyst does not require medium transport, and can directly act on gravity) Lower the riser into the catalyst replenishment zone);
  • the catalytic cracking reaction process is as follows:
  • reaction oil and gas The hydrocarbons (reaction oil and gas) produced by the catalyst and catalytic cracking reaction enter the catalyst splitting zone upwards, and some of the catalysts are tangentially diverted by gas-solid outward swirling and flow downward into the catalyst stripping zone by gravity to maintain the oil and gas (reaction). Catalysts remain in the oil and gas; the un-flowed catalyst and oil and gas (reaction oil and gas) continue to flow upwards, and enter the oil-gas re-reaction zone (or into the oil-gas re-reaction zone for mixing) together with the regenerated catalyst entering the catalyst replenishment zone.
  • the catalytic re-reaction of the oil and gas is carried out; after the catalytic re-reaction is completed, the oil and gas and the catalyst in the riser reactor are separated in the settler, and the oil and gas enters the fractionation tower system through the oil and gas pipeline, the feedstock oil reaction zone and the oil and gas re-reaction zone.
  • the spent catalyst is steam stripped in the stripping section of the catalyst to be produced, and (from the catalyst riser) enters the regenerator to recover activity.
  • the reaction conditions of the reaction zone of the feedstock oil are controlled to be: a reaction temperature of 510-550 ° C, a reaction time of 0.4-0.8 s, and an average flow velocity of the oil and gas of 5.0-20 m/s. More preferably, the reaction temperature is controlled to be 520 to 540 °C.
  • the temperature or the mixing temperature of the regenerated catalyst of the pre-lifting section is controlled to be 620 to 700 °C.
  • the temperature of the regenerative catalyst (adjusted by the regenerated catalyst temperature controller) entering the catalyst replenishing zone is controlled to be 490-650 °C. More preferably, the temperature is controlled to be 530-600 °C.
  • the reaction temperature of the oil-gas rereaction zone is controlled to be 490-515 °. C, the reaction time is controlled to be 0.6-1.2S; in the catalytic cracking reaction (chemical-type catalytic cracking reaction) for the purpose of low-carbon olefin yield, the reaction temperature of the oil-gas re-reaction zone is controlled to 530-630 ° C, reaction time The control is 1.0-2.0s.
  • refinery oil may also enter the feedstock oil reaction zone or the oil and gas re-reaction zone to participate in catalytic cracking, and a quenching medium may be provided in the oil and gas re-reaction zone for controlling the reaction of the oil and gas re-reaction zone.
  • a quenching medium may be provided in the oil and gas re-reaction zone for controlling the reaction of the oil and gas re-reaction zone.
  • the refinery oil and the feedstock oil may be fed in the feedstock reaction zone or the refinery oil may be fed in the oil and gas rereaction zone, preferably the refinery oil is fed in the oil and gas re reaction zone; the feed mode may be separately fed into the oil and gas.
  • Material, or feedstock oil is fed in the lower part of the feedstock reaction zone, and the refinery oil is fed at the appropriate position in the upper part of the feedstock feed port, or the feedstock oil is fed in the feedstock reaction zone, and the refinery is fed in the oil and gas re reaction zone.
  • the method can be adjusted according to the nature of the raw materials and the process requirements; accordingly, one to many rows of feed nozzles can be arranged at appropriate positions of the riser reactor. It can be adjusted according to the nature of the raw materials and process requirements to meet the needs of raw material changes.
  • the gas flow rate of the first regeneration zone of the regeneration section is controlled to be 1.5 - 3.0 m / s.
  • the feedstock oil reaction zone of the riser reactor and the catalyst to be produced in the oil-gas rereaction zone share a stripping zone or a stripping zone respectively; the catalyst after stripping Regeneration of the regenerator through the riser.
  • the riser is placed between the stripping zone (stripping section) and the regenerator and is typically connected to the bottom of the regenerator.
  • the catalyst which is partially reacted in the oil-gas re-reaction zone is returned to the oil-gas re-reaction zone by gravity, and is circulated in the oil-gas re-reaction zone to increase the catalyst of the oil-gas re-reaction zone. Reserve or reduce the reaction space velocity.
  • the amount of the catalyst to be produced entering the oil-gas rereaction zone in the feed oil reaction zone of the riser reactor is controlled according to the carbon content of the catalyst in the oil-reactor reaction zone; 5-40% of the catalyst to be produced enters the oil and gas re-reaction zone. More preferably, 15-25% of the starting catalyst in the feedstock reaction zone enters the hydrocarbon rereaction zone.
  • the present invention also provides a catalytic cracking unit which can be used in the catalytic cracking method provided by the present application, comprising a riser reactor, a settler, a stripping section and a regenerator, the settler setting At the top of the riser reactor, the regenerator is connected to the riser reactor via a line, wherein:
  • the riser reactor is provided with a pre-lifting section, a feedstock oil reaction zone, and an oil-gas re-reaction zone from bottom to top, and a catalyst splitter is disposed outside the outlet of the feedstock reaction zone; the oil-gas re-reaction zone is disposed in the Above the stripping section, the stripping section is coaxial or juxtaposed with the feedstock reaction zone;
  • the regenerator is coaxially disposed with a lower first regeneration zone, a middle dense phase fluidized bed zone and an upper dilute phase catalyst sedimentation separation zone, the three zones being coaxially disposed, the first regeneration zone and the A partition is disposed between the dense phase fluidized bed zones, and the height of the first regeneration zone is 18-26 m ;
  • the catalytic cracking unit further includes a regenerated catalyst temperature controller or a cooler, and a regenerative catalyst inlet pipe is disposed between the catalyst temperature controller or the cooler and the dense phase fluidized bed zone of the regenerator, the catalyst temperature controller or a cooling regeneration catalyst line is disposed between the cooler and the riser reactor, and a sliding raft is disposed on the cooling regeneration catalyst pipeline;
  • a distribution plate is arranged in a lower portion of the oil and gas re-reaction zone of the riser reactor, the distribution plate is provided with an opening or a passage, and a communication port is arranged on a side wall of the oil and gas re-reaction zone (a low temperature regenerated catalyst pipeline and an oil and gas re reaction zone) Through the communication port, the region between the communication port and the distribution plate is a catalyst supplemental distribution zone, and the feedstock reaction zone
  • the area between the outlet and the distribution plate is a catalyst splitting zone; or, the lower part of the oil and gas re-reaction zone is provided with an upper partition plate and a lower partition plate, and the upper partition plate and the lower partition plate are provided with passages
  • the lower partition plate is provided with an ascending passage from the reaction zone of the feedstock oil (for catalyst and oil and gas streams), and the upper partition plate is provided with an ascending passage communicating with the oil and gas re-reaction zone (for the above raw materials)
  • a catalyst return pipe is disposed, the catalyst return pipe is provided with a slipper; or a second stripping section is disposed in the oil and gas re-reaction zone, the second stripping section It is coaxial or juxtaposed with the oil and gas re-reaction zone.
  • a catalyst circulation pipe is disposed between the settler and the oil-gas rereaction zone or between the second stripping section and the oil-gas re-reaction zone, and the catalyst circulation pipe is disposed on the catalyst circulation pipe
  • the slipper is used to return the spent catalyst after partial reaction of the oil and gas re-reaction zone to the oil and gas re-reaction zone.
  • the number and cross-sectional area of the opening or the passage of the distribution plate are designed by controlling the oil and gas line speed at 20-30 m/s, that is, the layout of the opening or the channel is provided.
  • the number and cross-sectional area meet the requirements of oil and gas line speed 20-30m/s.
  • the catalyst temperature controller or the cooler is designed to achieve flexible adjustment of the temperature of the catalyst entering the riser reactor, and the internal structure design of the catalyst temperature controller is preferably selected from the catalyst cooling device described in ZL200920223355.1.
  • the full text is incorporated herein by reference; in addition, corresponding gas distributors are provided as needed in the respective regions such as the stripping section, the distribution plate, the catalyst supplemental distribution zone, and the catalyst temperature controller.
  • the technical scheme of the present invention is realized as follows: the regenerated catalyst from the regenerator is reacted with the preheated feedstock in the reaction zone of the reactor feedstock, and the reaction mixture flows upward along the reactor into the catalyst split zone, and a part of the reaction is awaiting The catalyst is separated into the stripping section, and the remaining reactant streams continue to enter the oil and gas re-reaction zone, and are mixed with a regenerated catalyst cooled by the catalyst temperature controller to a suitable temperature to carry out catalytic re-reaction; after the reaction, the oil and gas and the catalyst Entering the settler for separation, the oil and gas enters the fractionation system through the oil and gas outlet, and the catalyst enters the stripping section for stripping and then returns to the regenerator for regeneration.
  • the catalyst to be produced in the reaction zone of the feedstock oil is diverted before entering the oil and gas re-reaction zone, thereby controlling the ratio of the spent catalyst entering the hydrocarbon re-reaction zone to the regenerated catalyst added to the re-reaction zone of the oil and gas, and achieving the overall oil and gas Control of catalyst flow rate and catalyst activity in the re-reaction zone to achieve the goal of improving product distribution and product quality;
  • the inlet elevation of the regenerated catalyst into the pre-lift section of the reactor and the catalyst replenishment zone is lower than the elevation of the regenerative catalyst from the outlet of the regenerated catalyst temperature controller, and the catalyst is introduced into the pre-reduction by gravity.
  • the lifting section and the catalyst supplementary distribution zone do not need to raise the medium;
  • the second stripping section is set up to regenerate the catalyst after the cracking reaction of the feedstock reaction zone and the catalyst to be produced after the cracking reaction of the oil and gas re-reaction zone in the stripping section and the second stripping section.
  • Different stripping conditions can be set according to the process requirements, which is beneficial to the operation of the device.
  • FIG. 1 is a schematic structural view of a catalytic cracking apparatus provided in Embodiment 1;
  • FIG. 2 is a schematic structural view of a catalytic cracking device provided in Embodiment 2;
  • Embodiment 3 is a schematic structural view of a catalytic cracking device provided in Embodiment 3;
  • FIG. 4 is a schematic structural view of a catalytic cracking device provided in Embodiment 4.
  • Figure 5 is a schematic structural view of a catalytic cracking device provided in Embodiment 5;
  • Figure 6 is a schematic view showing the structure of a catalytic cracking apparatus provided in Example 6. Main component symbol description:
  • Example 1 The detailed description of the technical features of the present invention is intended to be illustrative of the preferred embodiments of the invention.
  • the embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 1.
  • the catalytic cracking device comprises a reaction portion and a regeneration portion, and the reaction portion comprises a riser reactor and a stripping zone. And settler
  • the regeneration part comprises a regenerator and a catalyst temperature controller or a cooler, wherein
  • the riser reactor is from the bottom to the top, the pre-lift section ring, the feedstock reaction zone I, the catalyst split zone III, and the oil and gas re-reaction zone II ;
  • a feed nozzle 1 is arranged on the side wall of the bottom of the feed oil reaction zone I, a catalyst splitter 4 is arranged at the outlet of the feed oil reaction zone I, and the outer side of the feed oil reaction zone I is a stripping section 7 (ie, awaiting a catalyst stripping zone V), the stripping section 7 is disposed coaxially with the feedstock oil reaction zone I;
  • the riser reactor is further provided with a second stripping section 11 and a second stripping section 11 (the catalyst stripping zone VD is coaxial with the oil-gas re-reaction zone II;
  • the oil and gas re-reaction zone is disposed above the stripping section 7, and the upper part of the oil-gas re-reaction zone II is provided with an upper baffle and a lower baffle, and the upper baffle and the lower baffle are respectively provided with a baffle passage 3, that is, a catalyst splitting zone a channel between III and the hydrocarbon re-reaction zone II, the periphery of the separator channel 3 is a catalyst supplemental distribution zone IV;
  • the settler VI is located at the upper part of the stripping section 7, and is provided with an oil and gas outlet 8;
  • the regenerator 13 of the regeneration portion is coaxially disposed with a lower first regeneration zone 17, a dense phase fluidized bed zone 18 in the middle, and a thin phase catalyst sedimentation zone 19 in the upper portion, a first regeneration zone 17 and a dense phase fluidized bed zone.
  • a partition 20 is disposed between the 18; a top of the regenerator 13 is provided with a flue gas outlet 14 for discharging flue gas in the regenerator 13;
  • a regenerated catalyst inlet pipe 23 is disposed between the catalyst temperature controller 21 and the dense phase fluidized bed zone 18 of the regenerator 13, and a temperature reduction regenerated catalyst line 22 is disposed between the catalyst replenishment zone IV of the lift reactor and is regenerated at a low temperature.
  • the catalyst line 22 is provided with a sliding raft, and the low-temperature regenerated catalyst line 22 is connected to the catalyst replenishing distribution area IV through the communication port 24, and the communication port 24 is disposed on the side wall of the catalyst replenishing distribution area IV;
  • the bottom of the pre-lifting section ring communicates with the dense phase fluidized bed zone 18 of the regenerator 13 through the regeneration riser 15, and the bottom of the stripping section 7 communicates with the bottom of the regenerator 13 through the standby riser 9, the second stripping section
  • the bottom of the 11 is in communication with the bottom of the regenerator 13 through the riser 10 to be raised.
  • the device design principle of the catalyst temperature controller 21 is the same as that of the catalyst cooler, but the catalyst temperature controller 21 is set to control the temperature of the regenerated catalyst, and the catalyst is controlled by the catalyst temperature controller 21. It is directly into the reactor to participate in the catalytic reaction; and the catalyst cooler is set to remove excess heat from the reaction regeneration system, without controlling the temperature of the regenerated catalyst, and the catalyst cooled by the catalyst cooler is returned to the regenerator.
  • the setting purpose of the catalyst temperature controller the following embodiments are the same as this type, and are no longer one by one. Description.
  • This embodiment also provides a catalytic cracking method which is carried out by using the above catalytic cracking apparatus, and comprises the following steps:
  • the regenerated catalyst from about 690 ° C in the dense phase fluidized bed zone 18 flows into the pre-lifting section ring along the regeneration riser 15 and is mixed with the heavy oil which is preheated to 220 ° C and atomized by the feed nozzle 1 into the riser reaction.
  • the reaction zone I of the feedstock oil it flows upward along the reaction zone I of the feedstock and continuously reacts, the reaction time is 0.8s, and the reaction temperature is 520 °C ;
  • the reaction mixture is separated upward by the catalyst splitter 4, and the separated catalyst enters the stripping section 7 and is stripped, and then enters the regenerator 13 along the waiting riser 9 for regeneration.
  • the oil and gas and the unseparated catalyst pass through the separator channel 3 upward.
  • the low-temperature regenerated catalyst extracted from the catalyst temperature controller 21 enters the oil-reactor reaction zone II along the low-temperature regeneration catalyst line 22 through the catalyst distribution zone IV, and the above-mentioned feedstock oil entering the oil-gas re-reaction zone II
  • the reaction oil and reaction catalyst of reaction zone I are mixed and continue to react, the reaction temperature is 510 ° C, and the reaction time is 0.6 s;
  • the oil and gas enters the settler VI, and the oil separated from the catalyst is taken out through the oil and gas outlet 8, and the raw catalyst flows into the second stripping section 11, and the oil and gas entrained in the stripped catalyst is passed through the riser 10
  • the return regenerator 13 is regenerated, and the regenerated flue gas is discharged from the flue gas outlet 14.
  • the single-pass conversion rate of the above catalytic cracking reaction by the catalytic cracking unit provided in the present embodiment is increased by an average of 10% or more, and the liquid recovery is increased by about 2%.
  • the present embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 2, wherein the stripping section 7 is disposed coaxially with the feedstock oil reaction zone I, and the second stripping section 11 and the oil and gas re
  • the reaction zone II is arranged side by side; a catalyst circulation pipe 12 is disposed between the settler VI and the catalyst supplementary distribution zone IV, and a part of the catalyst to be returned is returned to the hydrocarbon re-reaction zone II to participate in the reaction.
  • the rest of the device structure is the same as in Embodiment 1.
  • the present embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 3, wherein the stripping section 7 is juxtaposed with the feedstock oil reaction zone I, and the second stripping section 11 is reacted with oil and gas. Zone II is juxtaposed; a catalyst circulation pipe 12 is disposed between the settler VI and the catalyst replenishment zone IV, and a portion of the catalyst to be returned is returned to the hydrocarbon re-reaction zone II to participate in the reaction.
  • the rest of the device structure is the same as in Embodiment 1.
  • the present embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 4, wherein a distribution plate 2 is disposed in the lower portion of the oil and gas re-reaction zone II, and the distribution plate 2 is provided with a plurality of openings or Channel; reaction part does not include the first
  • the second stripping section 11 ie, the catalyst stripping zone VD; the stripping section 7 and the feedstock oil reaction zone I are coaxially arranged, the oil and gas re-reaction zone II and the feedstock oil reaction zone I share the stripping section 7, in the settler VI
  • a catalyst reflux pipe 6 is disposed, and the catalyst to be produced after the reaction of the hydrocarbon re-reaction zone II is introduced into the stripping section 7 through the return pipe 6 for stripping and then regenerated into the regenerator 13.
  • Regeneration part structure Same as Example 1.
  • This embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 5, wherein a regeneration riser 16 is disposed between the catalyst temperature controller 21 and the pre-lifting section ring, and the regeneration riser is provided. A slider is provided on the 16; the rest of the device structure is the same as in the second embodiment.
  • two catalyst streams entering the pre-lifting section ring the regenerated catalyst directly discharged from the regeneration riser 15 and the temperature-regulated controller 21 are adjusted to cool down.
  • the regenerated catalyst, the two catalysts are mixed in the pre-lifting section ring and then flow upward to participate in the catalytic reaction.
  • This embodiment provides a catalytic cracking device (reverse-re-device), the structure of which is shown in FIG. 6, wherein the device structure is the same as that of the embodiment 1, but the upper portion of the standby pipe 16 connected to the pre-lifting segment ring is not Directly in communication with the dense phase fluidized bed zone 18 of the regenerator 13, it is in communication with the catalyst temperature controller 21.
  • the catalyst stream entering the pre-lifting section ring is a regenerated catalyst which is adjusted to be cooled by the catalyst temperature controller 21.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

提供一种催化裂化方法，该方法包括：使进入预提升段（VIII）的再生催化剂与原料油混合并进入原料油反应区（I），进行催化裂化反应；催化剂和油气向上进入催化剂分流区（III），使部分催化剂分流并流入待生催化剂汽提区（V，VII）；未被分流的催化剂和油气继续向上流动，与进入催化剂补充分配区（IV）的再生催化剂一起进入油气再反应区（II）混合并进行油气的催化再反应；然后，提升管反应器内的油气和催化剂在沉降器（VI）内实现气固分离，油气经油气管线进入分馏塔系统，原料油反应区（I）和油气再反应区（II）的待生催化剂在待生催化剂气提段内经蒸汽汽提后，进入再生器（13）回复活性。还提供了一种用于上述催化裂化方法的催化裂化装置。

Description

一种催化裂化方法及装置 技术领域
本发明涉及一种催化裂化方法及装置，特别是涉及一种石油烃类原料催化裂化方法 及装置， 属于石油化工技术领域。 背景技术
催化裂化装置是最主要的汽油生产装置， 世界绝大部分车用汽油来自催化裂化装 置， 常规催化裂化采用提升管反应器。
现有提升管反应器的最大弊端是提升管过长，提升管出口处的催化剂活性只有初始 活性的 1/3左右， 因此， 在提升管反应器的后半段， 催化剂活性及选择性已急剧下降， 催化作用变差， 热裂化反应及其他不利二次反应增加， 不但限制了单程转化率的提高， 同时导致催化汽油烯烃含量高达 45%以上， 远不能满足汽油的新标准要求。 随着催化剂 活性的降低， 催化反应的选择性必然下降， 副反应自然增加。
要提高催化过程的单程转化率， 核心问题是提高现有提升管反应器后半段的催化剂 活性， 中国专利申请 99213769.1公开了一种用于催化裂化的两段串联式装置，该装置由 两结构相同的催化裂化装置上下头尾相接重叠而成， 该技术通过采用上下重叠的反应、 再生装置， 通过缩短反应时间强化了常规提升管催化裂化反应过程， 从而提高了催化剂 的有效活性和选择性。 但是， 该专利申请公开的技术仅限于原理， 缺乏可操作的实施办 法， 工程实施时相当于建设两套上下重叠的催化裂化反应再生装置， 投资费用高， 实施 可能性很小。
中国专利申请 00122845.5公开了一种烃油的两段催化裂化方法，使烃油首先在第一 反应器中与裂化催化剂接触并反应，所生成的油气送入第二反应器中与含有五元环高硅 沸石的催化剂接触并反应， 所生成的油气送入分馏塔进行分离。 该方法两反应器中的催 化剂是组成和性质不同的催化剂， 虽然使第一反应器的反应油气与第二反应器中的新鲜 催化剂接触， 提高了第二反应器中的产品选择性， 但该方法采用了两种催化剂， 两套并 列的反应 -再生系统， 投资费用较高。
中国专利申请 00134054.9公开了一种两段提升管催化裂化新技术，将提升管分为上 下两段， 第一区催化剂来自再生器， 第一区反应结束， 催化剂、 油气通过设置在第一区 末端的中间分流器分离， 仅油气继续进入第二反应段反应； 第二反应段的催化剂为来自 再生器的经过外取热器取热的再生催化剂。 该技术是在反应第二段 （即提升管后半段） 用高活性的经冷却的低温再生催化剂与油气继续接触反应， 提高了第二段的催化剂活 性， 提高了单程转化率。 但该技术中第一区分离出来的催化剂在进入再生器前必须经过 汽提， 同时再生催化剂必须由输送介质向上输送才能进入第二段， 汽提蒸汽、 输送介质 将全部进入第二段提升管， 势必影响到第二段的反应； 若限制汽提蒸汽量， 则会影响到 汽提效果，进而影响再生过程；此外，从外取热器底部到第二反应段入口高度差几十米， 输送介质量很大， 需要消耗大量能耗； 且该技术需要两个沉降器， 两个汽提段， 投资大 幅增加。 发明内容
为解决上述问题， 本发明的目的在于提供一种新的催化裂化方法， 该方法既能改善 产品分布和产品质量， 又能降低工程投资和方便工程实施。
本发明的目的还在于提供一种用于上述催化裂化方法的催化裂化装置。
为达到上述目的， 本发明首先提供了一种催化裂化方法， 催化裂化反应在设置有一 个提升管反应器的反应部分和包括再生器的再生部分的反-再装置中进行， 其中：
所述反应部分由提升管反应器、 待生催化剂汽提区及沉降器组成； 所述提升管反应 器包括自下而上的预提升段、 原料油反应区、 催化剂分流区、 催化剂补充分配区和油气 再反应区； 所述催化剂分流区设置在所述原料油反应区的出口处； 所述催化剂分流区和 油气再反应区之间设有通道， 该通道外围为所述催化剂补充分配区；
所述再生器自下而上设有下部的第一再生区、 中部的密相流化床区和上部的稀相催 化剂沉降分离区； 所述第一再生区和所述中部密相流化床区之间可以用隔板（例如带有 通道的隔板） 分开；
来自所述再生器中部的密相流化床区的再生催化剂按以下方式分别进入所述提升 管反应器的预提升段和催化剂补充分配区：
进入预提升段： 再生催化剂直接依靠重力向下进入预提升段（该预提升段位于提升 管反应器的原料油反应区的喷嘴下方）， 或者再生催化剂先降温 （可以使再生催化剂在 重力作用下进入催化剂温度控制器或冷却器进行降温）后再靠重力进入预提升段（可以 依靠重力向下而进入）， 或者再生催化剂和降温后的再生催化剂分两路同时进入预提升 段 （可以依靠重力向下而进入）；
进入催化剂补充分配区： 再生催化剂在降温（可以使再生催化剂在重力作用下进入 催化剂温度控制器进行降温）后靠重力进入所述催化剂补充分配区（再生催化剂不需要 介质输送， 可以直接在重力作用下经立管向下进入催化剂补充分配区）； 所述催化裂化反应流程如下：
使进入预提升段的再生催化剂与预热的反应原料油接触混合并沿提升管反应器向 上进入原料油反应区， 进行催化裂化反应；
催化剂和催化裂化反应所产生的油气 （反应油气） 向上进入催化剂分流区， 采用气 固向外旋流方式使部分催化剂切向分流并靠重力向下流入待生催化剂汽提区，保持油气 (反应油气） 中留存有催化剂； 未被分流的催化剂和油气 （反应油气） 继续向上流动， 与进入催化剂补充分配区的再生催化剂混合一起进入油气再反应区（或者说一起进入油 气再反应区进行混合）并进行油气的催化再反应； 完成催化再反应后， 提升管反应器内 的油气和催化剂在沉降器内实现气固分离， 油气经油气管线进入分馏塔系统， 原料油反 应区和油气再反应区的待生催化剂在待生催化剂汽提段内经蒸汽汽提后， （自催化剂立 管） 进入再生器回复活性。
在本发明所提供的上述催化裂化方法中，优选地，原料油反应区的反应条件控制为： 反应温度 510-550 °C、 反应时间 0.4-0.8s、 油气平均流速 5.0-20m/s。 更优选地， 反应温 度控制为 520-540 °C。
在本发明所提供的上述催化裂化方法中， 优选地， 预提升段的再生催化剂的温度或 混合温度控制为 620-700°C。
在本发明所提供的上述催化裂化方法中， 优选地， 进入催化剂补充分配区的再生催 化剂 （经再生催化剂温度控制器调节） 降温的温度控制为 490-650°C。 更优选地， 该温 度控制为 530-600°C。
在本发明所提供的上述催化裂化方法中， 优选地， 在以汽柴油收率为目的的催化裂 化反应 （油品型催化裂化反应） 中， 油气再反应区的反应温度控制为 490-515 °C， 反应 时间控制为 0.6-1.2S; 在以低碳烯烃收率为目的的催化裂化反应（化工型催化裂化反应) 中， 油气再反应区的反应温度控制为 530-630°C， 反应时间控制为 1.0-2.0s。
上述催化裂化方法中， 回炼油等其他烃类组分也可以进入原料油反应区或油气再反 应区参与催化裂化， 还可以在油气再反应区设置急冷介质， 用于控制油气再反应区的反 应时间。 具体地， 可以使回炼油与原料油在原料油反应区进料或者使回炼油在油气再反 应区进料， 优选使回炼油在油气再反应区进料； 进料方式可采用原料油单独进料， 或者 原料油在原料油反应区下部进料、 回炼油在原料油进料口上部适当位置进料， 或者原料 油在原料油反应区进料、回炼油在油气再反应区进料等灵活方式，具体可根据原料性质、 工艺要求进行调整；相应地，可以在提升管反应器的适当位置设置一排到多排进料喷嘴， 具体可根据原料性质、 工艺要求进行调整， 以适应原料变化需要。
在本发明所提供的上述催化裂化方法中， 优选地， 再生部分的第一再生区的气体流 速控制为 1.5-3.0m/s。
在本发明所提供的上述催化裂化方法中， 优选地， 提升管反应器的原料油反应区和 油气再反应区的待生催化剂共用一个汽提区或分别设置汽提区； 汽提后的催化剂经立管 进入再生器再生。 该立管设置于汽提区 （汽提段）与再生器之间， 一般是连接到再生器 的底部。
在本发明所提供的上述催化裂化方法中， 优选地， 部分在油气再反应区反应后的待 生催化剂靠重力返回油气再反应区内， 在油气再反应区循环， 增加油气再反应区的催化 剂藏量或降低反应空速。
在本发明所提供的上述催化裂化方法中， 优选地， 提升管反应器的原料油反应区的 待生催化剂进入油气再反应区的量根据油气再反应区催化剂的含碳量控制； 原料油反应 区待生催化剂的 5-40%进入油气再反应区。 更优选地， 原料油反应区待生催化剂的 15-25%进入油气再反应区。
本发明还提供了一种催化裂化装置， 该催化裂化装置可以用于本申请所提供的催化 裂化方法， 其包括一个提升管反应器、 沉降器、 汽提段和再生器， 所述沉降器设置在所 述提升管反应器的顶部， 所述再生器通过管线与所述提升管反应器连接， 其中：
所述提升管反应器自下而上设置有预提升段、 原料油反应区、 油气再反应区， 所述 原料油反应区出口外设置有催化剂分流器； 所述油气再反应区设置在所述汽提段上方， 所述汽提段与所述原料油反应区同轴或并列设置；
所述再生器同轴设置有下部的第一再生区、 中部的密相流化床区和上部的稀相催化 剂沉降分离区， 这三个区为同轴设置， 所述第一再生区和所述密相流化床区之间设置有 隔板， 所述第一再生区的高度为 18-26m;
该催化裂化装置还包括再生催化剂温度控制器或冷却器， 该催化剂温度控制器或冷 却器与所述再生器的密相流化床区之间设置有再生催化剂进入管， 该催化剂温度控制器 或冷却器与所述提升管反应器之间设置有降温再生催化剂管线，在该降温再生催化剂管 线上设置有滑闽；
所述提升管反应器的油气再反应区下部设有分布板， 该分布板设有开口或通道， 所 述油气再反应区的侧壁上设有连通口（低温再生催化剂管线与油气再反应区通过该连通 口连通）， 该连通口与所述分布板之间的区域为催化剂补充分配区， 所述原料油反应区 的出口与所述分布板之间的区域为催化剂分流区； 或者， 所述油气再反应区的下部设有 上隔板和下隔板， 所述上隔板和下隔板上均设有通道， 其中， 所述下隔板设有一个来自 原料油反应区的上升通道 （供催化剂和油气物流上升用）， 所述上隔板设有一个与油气 再反应区连通的上升通道（供上述原料油反应区物流和补充的降温催化剂物流上升用）， 所述上隔板、 下隔板之间和所述通道外的区域为催化剂补充分配区， 所述低温再生催化 剂管线与该催化剂补充分配区通过催化剂补充分配区侧壁的连通口连通， 原料油反应区 出口与所述下隔板之间的区域为催化剂分流区；
在所述沉降器与所述汽提段之间设置有催化剂回流管，该催化剂回流管上设置有滑 闽； 或者在所述油气再反应区设置第二汽提段， 该第二汽提段与所述油气再反应区同轴 或并列设置。
在本发明提供的上述催化裂化装置中， 优选地， 沉降器与油气再反应区之间或者第 二汽提段与油气再反应区之间设有催化剂循环管， 在该催化剂循环管上设有滑闽， 用于 使部分油气再反应区反应后的待生催化剂返回油气再反应区内。
在本发明提供的上述催化裂化装置中， 优选地， 分布板设置开口或通道的个数及截 面积通过控制油气线速在 20-30m/s进行具体工艺设计，即布板设置开口或通道的个数及 截面积满足油气线速 20-30m/s的要求。
在本发明中，催化剂温度控制器或冷却器的设计可以实现对进入提升管反应器中的 催化剂温度的灵活调节，催化剂温度控制器的内部结构设计优先选用 ZL200920223355.1 中所述的催化剂降温设备， 将其全文引入这里作为参考； 此外， 在汽提段、 分布板、 催 化剂补充分配区及催化剂温度控制器等相应区域均根据需要设置相应的气体分布器。
本发明的技术方案是这样实现的： 来自再生器的再生催化剂在反应器原料油反应区 与预热的原料油接触反应， 反应混合物沿反应器向上流动进入催化剂分流区， 一部分反 应过的待生催化剂分流出来进入汽提段， 其余反应物流则继续向上进入油气再反应区， 与一部分经催化剂温度控制器冷却降温至适宜温度的再生催化剂混合后，进行催化再反 应； 反应结束后， 油气和催化剂进入沉降器进行分离， 油气经油气出口进入分馏系统， 催化剂则进入汽提段进行汽提后返回再生器再生。
本发明的技术方案具有以下有益效果：
1、 由于向油气再反应区补充的是高活性的低温再生催化剂， 总体上强化了整个提 升管反应器中的催化活性及反应选择性，有效抑制了热反应，可使反应总液收增加 1.0% 以上； 2、 原料油反应区的待生催化剂在进入油气再反应区之前先进行分流， 从而控制进 入油气再反应区的待生催化剂与补充进入油气再反应区的再生催化剂的比例，整体上实 现对油气再反应区催化剂流量及催化剂活性的控制， 实现改善产品分布和产品质量的目 标；
3、 由于反-再装置的设计， 再生催化剂进入反应器预提升段和催化剂补充分配区的 入口标高均低于再生催化剂由再生催化剂温度控制器引出口的标高，催化剂靠重力自然 下降分别引入预提升段和催化剂补充分配区， 不需提升介质；
4、 第二汽提段的设置可以使原料油反应区裂化反应后的待生催化剂、 油气再反应 区裂化反应后的待生催化剂分别在汽提段、 第二汽提段进行汽提后再生， 可根据工艺需 要设置不同的汽提条件， 利于装置操作。 附图说明
图 1为实施例 1提供的催化裂化装置的结构示意图；
图 2为实施例 2提供的催化裂化装置的结构示意图；
图 3为实施例 3提供的催化裂化装置的结构示意图；
图 4为实施例 4提供的催化裂化装置的结构示意图；
图 5为实施例 5提供的催化裂化装置的结构示意图；
图 6为实施例 6提供的催化裂化装置的结构示意图。 主要组件符号说明：
进料喷嘴 1 分布板 2 隔板通道 3 催化剂分流器 4 催化剂回流管 6 汽提段 7 油气出口 8 待生立管 9,10 第二汽提段 11 催化剂循环管 12 再生器 13 烟气出口 14 再生立管 15,16 第一再生区 17 密相流化床区 18 催化剂沉降分离区 19 隔板 20 催化剂温度控制器 21 低温再生催化剂管线 22 再生催化剂进入管 23 连通口 24 原料油反应区 I 油气再反应区 II 催化剂分流区 III 催化剂补充分配区 IV 待生催化剂汽提区 ν ,νπ 沉降器 VI 预提升段 環
具体实施方式
为了对本发明的技术特征、 目的和有益效果有更加清楚的理解， 现对本发明的技 术方案进行以下详细说明， 但不能理解为对本发明的可实施范围的限定。 实施例 1
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 1所示， 该催化裂化 装置包括一反应部分以及一再生部分， 反应部分包括一提升管反应器、 汽提区和沉降器
VI， 再生部分包括一再生器以及催化剂温度控制器或冷却器， 其中，
提升管反应器自下而上分别为预提升段環、 原料油反应区 I、 催化剂分流区 III、 油 气再反应区 II ;
在原料油反应区 I底部的侧壁上设有进料喷嘴 1， 在原料油反应区 I的出口处设有 催化剂分流器 4， 原料油反应区 I的外侧为汽提段 7 (即待生催化剂汽提区 V )， 汽提段 7与原料油反应区 I同轴设置；
提升管反应器还设置有第二汽提段 11， 第二汽提段 11 (待生催化剂汽提区 VD 与 油气再反应区 II同轴设置；
油气再反应区 Π设置在汽提段 7上方，油气再反应区 II的下部设有上隔板和下隔板， 上隔板和下隔板上均设有隔板通道 3，即催化剂分流区 III和油气再反应区 II之间的通道， 该隔板通道 3的外围为催化剂补充分配区 IV；
沉降器 VI位于汽提段 7的上部， 设有油气出口 8;
再生部分的再生器 13 同轴设置有下部的第一再生区 17、 中部的密相流化床区 18 和上部的稀相催化剂沉降分离区 19，第一再生区 17和密相流化床区 18之间设置有隔板 20； 再生器 13 的顶部设有烟气出口 14， 用于排出再生器 13中的烟气；
催化剂温度控制器 21与再生器 13的密相流化床区 18之间设置有再生催化剂进入 管 23， 与提升反应器的催化剂补充分配区 IV之间设置有降温再生催化剂管线 22， 在低 温再生催化剂管线 22上设置有滑闽，低温再生催化剂管线 22与催化剂补充分配区 IV通 过连通口 24连通， 该连通口 24设置于催化剂补充分配区 IV的侧壁上；
预提升段環的底部通过再生立管 15与再生器 13的密相流化床区 18连通，汽提段 7 的底部通过待生立管 9与再生器 13的底部连通，第二汽提段 11的底部通过待生立管 10 与再生器 13的底部连通。
本发明中，所述的催化剂温度控制器 21的设备设计原理与催化剂冷却器是相同的， 但催化剂温度控制器 21的设置目的是控制再生催化剂温度，经催化剂温度控制器 21控 温后的催化剂是直接进入反应器参与催化反应的； 而催化剂冷却器的设置目的是取走反 应再生系统的多余热量， 不控制再生催化剂温度， 经催化剂冷却器冷却后的催化剂是重 新返回再生器的。 关于催化剂温度控制器的设置目的， 以下实施例与此类同， 不再一一 说明。
本实施例还提供了一种催化裂化方法， 其是采用上述催化裂化装置进行的， 包括以 下步骤：
来自密相流化床区 18的 690°C左右的再生催化剂沿再生立管 15流入预提升段環中， 与预热至 220°C经进料喷嘴 1 雾化后的重油混合进入提升管反应器的原料油反应区 I 内， 沿原料油反应区 I向上流动并不断反应， 反应时间 0.8s， 反应温度 520°C ;
反应混合物向上由催化剂分流器 4进行分离， 分离出的催化剂进入汽提段 7中汽提 后沿待生立管 9进入再生器 13中进行再生， 油气及未分离的催化剂经隔板通道 3向上 进入油气再反应区 Π内； 同时， 自催化剂温度控制器 21 引出的低温再生催化剂沿低温 再生催化剂管线 22经催化剂分配区 IV进入油气再反应区 II， 与进入油气再反应区 II的 上述原料油反应区 I的反应油气及待生催化剂接触混合并继续反应， 反应温度 510°C， 反应时间 0.6s;
反应结束后， 油气进入沉降器 VI内， 分离出催化剂的油气经油气出口 8引出， 待生 催化剂则流入第二汽提段 11内， 汽提出的催化剂中夹带的油气， 经待生立管 10返回再 生器 13再生， 再生烟气由烟气出口 14排出。
与现有技术相比，采用本实施例提供的催化裂化装置所进行的上述催化裂化反应的 单程转化率平均提高 10%以上， 液收增加 2%左右。
实施例 2
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 2所示， 其中， 汽提 段 7与原料油反应区 I同轴设置， 第二汽提段 11与油气再反应区 II并列设置； 在沉降 器 VI与催化剂补充分配区 IV之间设置有催化剂循环管 12，使部分待生催化剂返回油气再 反应区 II内参与反应。 其余部分装置结构同实施例 1。
实施例 3
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 3所示， 其中， 汽提 段 7与原料油反应区 I并列设置， 第二汽提段 11与油气再反应区 II并列设置； 在沉降 器 VI与催化剂补充分配区 IV之间设置有催化剂循环管 12，使部分待生催化剂返回油气再 反应区 II内参与反应。 其余部分装置结构同实施例 1。
实施例 4
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 4所示， 其中， 在油 气再反应区 II下部设有分布板 2， 分布板 2上设有多个开口或通道； 反应部分不包括第 二汽提段 11 (即待生催化剂汽提区 VD; 汽提段 7与原料油反应区 I同轴设置， 油气再 反应区 II与原料油反应区 I共用汽提段 7， 在沉降器 VI和汽提段 7之间设置有催化剂回 流管 6， 使油气再反应区 II反应后的待生催化剂通过回流管 6进入汽提段 7进行汽提后 进入再生器 13中再生。 再生部分装置结构同实施例 1。
实施例 5
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 5所示， 其中， 在催 化剂温度控制器 21与预提升段環之间设置有再生立管 16， 再生立管 16上设置有滑闽； 其余部分装置结构同实施例 2。
在采用本实施例提供的催化裂化装置所进行的催化裂化反应中，进入预提升段環的 为两股催化剂物流： 直接经再生立管 15引出的再生催化剂和经过催化剂温度控制器 21 调节降温后的再生催化剂，两股催化剂在预提升段環混合均匀后再向上流动参与催化反 应。
实施例 6
本实施例提供了一种催化裂化装置 （反 -再装置）， 其结构如图 6所示， 其中， 装置 结构同实施例 1， 但是， 与预提升段環连接的待生立管 16上部不直接与再生器 13的密 相流化床区 18连通， 而是与催化剂温度控制器 21连通。
在采用本实施例提供的催化裂化装置所进行的催化裂化反应中，进入预提升段環的 催化剂物流为经过催化剂温度控制器 21调节降温后的再生催化剂。

Claims

权利要求书
1、 一种催化裂化方法， 催化裂化反应在设置有一个提升管反应器的反应部分和包 括再生器的再生部分的反-再装置中进行， 其中：
所述反应部分由提升管反应器、 待生催化剂汽提区及沉降器组成； 所述提升管反应 器包括自下而上的预提升段、 原料油反应区、 催化剂分流区、 催化剂补充分配区和油气 再反应区； 所述催化剂分流区设置在所述原料油反应区的出口处； 所述催化剂分流区和 油气再反应区之间设有通道， 该通道外围为所述催化剂补充分配区；
所述再生器自下而上设有第一再生区、 密相流化床区和稀相催化剂沉降分离区； 来自所述密相流化床区的再生催化剂按以下方式分别进入所述提升管反应器的预 提升段和催化剂补充分配区：
进入预提升段： 再生催化剂直接进入预提升段， 或者再生催化剂先降温后再靠重力 进入预提升段， 或者再生催化剂和降温后的再生催化剂分两路同时进入预提升段； 进入催化剂补充分配区： 再生催化剂在降温后靠重力进入所述催化剂补充分配区； 所述催化裂化反应流程如下：
使进入预提升段的再生催化剂与预热的反应原料油接触混合并沿提升管反应器向 上进入原料油反应区， 进行催化裂化反应；
催化剂和催化裂化反应所产生的油气向上进入催化剂分流区，采用气固向外旋流方 式使部分催化剂切向分流并靠重力向下流入待生催化剂汽提区，保持油气中留存有催化 剂； 未被分流的催化剂和油气继续向上流动， 与进入催化剂补充分配区的再生催化剂混 合一起进入油气再反应区并进行油气的催化再反应； 完成催化再反应后， 提升管反应器 内的油气和催化剂在沉降器内实现气固分离， 油气经油气管线进入分馏塔系统， 原料油 反应区和油气再反应区的待生催化剂在待生催化剂汽提段内经蒸汽汽提后，进入再生器 回复活性。
2、 根据权利要求 1所述的催化裂化方法， 其中， 所述原料油反应区的反应条件控 制为： 反应温度 510-550 °C、 反应时间 0.4-0.8s、 油气平均流速 5.0-20m/s。
3、 根据权利要求 2所述的催化裂化方法， 其中， 所述反应温度控制为 520-540°C。
4、 根据权利要求 1所述的催化裂化方法， 其中， 所述预提升段的再生催化剂的温 度或混合温度控制为 620-700°C。
5、 根据权利要求 1所述的催化裂化方法， 其中， 进入所述催化剂补充分配区的再 生催化剂降温的温度控制为 490-65CTC。
6、 根据权利要求 5所述的催化裂化方法， 其中， 所述温度控制为 530-600°C。
7、 根据权利要求 1所述的催化裂化方法， 其中， 在以汽柴油收率为目的的催化裂 化反应中， 油气再反应区的反应温度控制为 490-515 °C， 反应时间控制为 0.6-1.2s; 在以 低碳烯烃收率为目的的催化裂化反应中， 油气再反应区的反应温度控制为 530-630°C， 反应时间控制为 1.0-2.0s。
8、 根据权利要求 1所述的催化裂化方法， 其中， 所述再生部分的第一再生区的气 体流速控制为 1.5-3.0m/s。
9、 根据权利要求 1所述的催化裂化方法， 其中， 所述提升管反应器的原料油反应 区和油气再反应区的待生催化剂共用一个汽提区或分别设置汽提区； 汽提后的催化剂进 入再生器再生。
10、 根据权利要求 1所述的催化裂化方法， 其中， 部分在油气再反应区反应后的待 生催化剂靠重力返回油气再反应区内， 在油气再反应区循环， 增加油气再反应区的催化 剂藏量或降低反应空速。
11、 根据权利要求 1所述的催化裂化方法， 其中， 所述提升管反应器的原料油反应 区的待生催化剂进入油气再反应区的量根据油气再反应区催化剂的含碳量控制； 所述原 料油反应区待生催化剂的 5-40%进入油气再反应区。
12、 根据权利要求 11所述的催化裂化方法， 其中， 所述原料油反应区待生催化剂 的 15-25%进入油气再反应区。
13、 一种催化裂化装置， 其包括一个提升管反应器、 沉降器、 汽提段和再生器， 所 述沉降器设置在所述提升管反应器的顶部，所述再生器通过管线与所述提升管反应器连 接， 其中：
所述提升管反应器自下而上设置有预提升段、 原料油反应区、 油气再反应区， 所述 原料油反应区出口外设置有催化剂分流器； 所述油气再反应区设置在所述汽提段上方， 所述汽提段与所述原料油反应区同轴或并列设置；
所述再生器同轴设置有下部的第一再生区、 中部的密相流化床区和上部的稀相催化 剂沉降分离区， 所述第一再生区和所述密相流化床区之间设置有隔板， 所述第一再生区 的高度为 18-26m;
该催化裂化装置还包括再生催化剂温度控制器或冷却器， 该催化剂温度控制器或冷 却器与所述再生器的密相流化床区之间设置有再生催化剂进入管， 该催化剂温度控制器 或冷却器与所述提升管反应器之间设置有低温再生催化剂管线，在该降温再生催化剂管 线上设置有滑闽；
所述提升管反应器的油气再反应区下部设有分布板， 该分布板设有开口或通道， 所 述油气再反应区的侧壁上设有连通口， 该连通口与所述分布板之间的区域为催化剂补充 分配区， 所述原料油反应区的出口与所述分布板之间的区域为催化剂分流区； 或者， 所 述油气再反应区的下部设有上隔板和下隔板，所述上隔板和下隔板上均设有通道，其中， 所述下隔板设有一个来自原料油反应区的上升通道，所述上隔板设有一个与油气再反应 区连通的上升通道，所述上隔板、下隔板之间和所述通道外的区域为催化剂补充分配区， 所述低温再生催化剂管线与该催化剂补充分配区通过催化剂补充分配区侧壁的连通口 连通， 原料油反应区出口与所述下隔板之间的区域为催化剂分流区；
在所述沉降器与所述汽提段之间设置有催化剂回流管，该催化剂回流管上设置有滑 闽； 或者在所述油气再反应区设置第二汽提段， 该第二汽提段与所述油气再反应区同轴 或并列设置。
14、 根据权利要求 13所述的催化裂化装置， 其中， 所述沉降器与油气再反应区之 间或所述第二汽提段与油气再反应区之间设有催化剂循环管，在该催化剂循环管上设有 滑闽。
15、 根据权利要求 13所述的催化裂化装置， 其中， 所述分布板设置开口或通道的 个数及截面积满足油气线速 20-30m/s的要求。
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