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WO2014071842A1 - 一种反应区催化剂控制和再生剂净化取热冷却方法及装置 - Google Patents

一种反应区催化剂控制和再生剂净化取热冷却方法及装置 Download PDF

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Publication number
WO2014071842A1
WO2014071842A1 PCT/CN2013/086630 CN2013086630W WO2014071842A1 WO 2014071842 A1 WO2014071842 A1 WO 2014071842A1 CN 2013086630 W CN2013086630 W CN 2013086630W WO 2014071842 A1 WO2014071842 A1 WO 2014071842A1
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Prior art keywords
catalyst
regenerant
reactor
reaction
temperature
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English (en)
French (fr)
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石宝珍
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Priority to US14/441,227 priority Critical patent/US9428698B2/en
Publication of WO2014071842A1 publication Critical patent/WO2014071842A1/zh
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • 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
    • 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
    • B01J8/005—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
    • 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
    • B01J8/1863—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 followed by a downward movement outside the reactor and subsequently re-entering it
    • 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
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/62—Catalyst regeneration
    • 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
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • 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
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the invention relates to a catalytic reaction technology in the field of petroleum and chemical industry, in particular to a catalyst for controlling and regenerating a catalyst (regenerant) for cooling and purifying a catalyst in a catalytic reaction, and relates to a catalyst control and regeneration in a reaction zone for realizing the method
  • the agent purifies and takes the heat cooling device.
  • Catalysts are a core issue during the catalytic reaction, but the performance of the catalyst during the reaction is different from that of the unreacted catalyst. Taking the reaction of hydrocarbon or alcohol compounds as an example, the catalyst will be coked, alkaline components and metal contamination and passivation during the reaction, so that the performance of the catalyst in the actual reaction process is much lower than that before the reaction.
  • the reaction conditions such as the activity of the catalyst, the ratio of the reactant oil or the space velocity, the temperature difference of the reaction raw materials and the catalyst, and the temperature are all important factors affecting the reaction results.
  • the choice and control of the reaction conditions during the catalytic reaction is directly related to the reaction conversion rate and reaction selectivity.
  • the catalytic conversion reaction is taken as an example.
  • the dry gas pre-lifting technology, the mixed temperature control technology that changes the injection point of the raw material and the injection medium, the rapid separation technology in the exit zone, and the quenching termination technology all have reaction results.
  • the impact is obvious and has been well applied in industry. Improvement and control of catalyst performance during the reaction are also critical.
  • Many gas-solid reaction processes require solid phase materials such as catalyst cooling to improve the reaction conditions, especially for gas-solid reaction processes such as catalytic conversion reactions. Properly lowering the regenerated catalyst can increase the ratio of the agent to the oil, inhibit the thermal cracking reaction, and improve the product. distributed.
  • the liquid feedstock catalytic reaction using the tubular reactor has two reaction zones of liquid phase gasification contact reaction and gas phase reaction.
  • the temperature difference between the catalyst and the raw material in the liquid phase gasification reaction zone and the high temperature of the catalyst increase the thermal cracking reaction, increasing the proportion of by-products below C2, and affecting economic benefits.
  • No. 5,800,697 discloses a catalytic conversion reaction-regeneration method in which a catalyst cooling zone is arranged beside the regenerator, and the heat regenerant from the dense phase bed is exchanged from the outlet into the cooling zone to a suitable temperature, and then regenerated by a riser and a slipper.
  • the bottom of the tube reactor participates in the reaction, thereby making the reaction temperature an independent variable.
  • Chinese patent 200610113673.3 discloses a method for converting petroleum hydrocarbons. The hot regenerated catalyst is cooled by a cooler and returned to the bottom of the reactor to be in contact with the feedstock oil and subjected to a cracking reaction. The catalyst to be produced is stripped and sent to a regenerator for charring.
  • Chinese Patent No. 200710054738.6 discloses a regenerative catalyst temperature regulating device for a catalytic cracking device, a catalyst desuperheater is arranged beside the dense phase bed of the regenerator, a heat exchange tube is arranged in the catalyst desuperheater, and a flue gas return line is arranged in the upper part, along the catalyst The fluidizer is arranged in a vertical height section of the desuperheater, and the regenerated catalyst that has been cooled enters the pre-lift section of the riser reactor to participate in the reaction.
  • Chinese Patent No. 200710054738.6 discloses a regenerative catalyst temperature regulating device for a catalytic cracking device, a catalyst desuperheater is arranged beside the dense phase bed of the regenerator, a heat exchange tube is arranged in the catalyst desuperheater, and a flue gas return line is arranged in the upper part, along the catalyst The fluidizer is arranged in a vertical height section of the desuperheater, and the
  • 200710054737.1 also discloses a catalytic cracking device regenerative catalyst temperature regulating device, which is provided with a partition in the dense phase bed of the regenerator, and the dense phase bed of the regenerator is divided into two zones, one zone is a regenerated charred zone, and the other zone is another
  • the zone is a catalyst cooling zone
  • the lower part of the separator is provided with a catalyst inlet of the desuperheater
  • the heat exchanger tube is arranged in the catalyst cooling zone, and the regenerated catalyst which is cooled down enters the riser reactor pre-lifter to participate in the reaction.
  • the catalyst from the external heat extracter carries a certain amount of oxygen and regenerated flue gas, and this part of the oxygen enters the reactor and reacts with the reaction medium, and there is a problem that the oxygen entering the reactor affects the product.
  • the flue gas carried from the regenerated catalyst will increase the pressure of the rich air compressor and increase the energy consumption.
  • reaction catalyst control includes not only the catalyst temperature before the reaction, the contact temperature difference between the liquid phase gasification reaction zone, and the ratio of the agent to the oil, but also the control of the catalyst activity in the gas phase reaction zone and the ratio of the agent to the oil also have an important influence on the reaction effect.
  • the activity of the catalyst at the outlet of the existing riser reactor is only about 1/3 of the initial activity.
  • the activity and selectivity of the catalyst have decreased sharply, the catalytic effect is deteriorated, the thermal cracking reaction and other disadvantages.
  • Two The proportion of secondary reactions increases.
  • the selectivity of the catalytic reaction inevitably decreases, and the side reaction naturally increases. Controlling catalyst activity in the second half of the riser reactor is an important issue.
  • CN99213769. 1 discloses a two-stage tandem riser reactor for catalytic cracking, which is formed by connecting two risers and a tail end in series, and the technique is strengthened by using a two-stage relay type reaction device.
  • control of the catalyst during the reaction should also include catalyst control of the gas phase reaction zone, control of the state of the catalyst provided, and control of the catalyst carrier gas.
  • the temperature control of the catalyst entering the reactor is also critical when replenishing the catalyst to the gas phase reaction zone of the reactor.
  • This part of the catalyst affects the heat balance of the reaction and has an effect not only on the reaction outlet temperature but also on the contact gasification zone.
  • the reaction can only be improved if the catalyst temperature and reaction requirements are compatible.
  • a primary object of the present invention is to provide a reaction zone catalyst control and regenerant purification and heat removal method for achieving convenient and flexible control of multiple reactions in the reaction zone catalyst and reducing energy consumption.
  • Another object of the present invention is to provide an apparatus for implementing the above method.
  • the present invention provides a reaction zone catalyst control and regenerant heat removal method for use in a catalytic reaction process of a petroleum hydrocarbon feedstock or an alcohol feedstock.
  • the method comprises the control of the reaction and the control of the catalyst participating in the reaction, and has the following parts: a reactor, a catalyst regenerator, a liquid phase contact gasification reaction control method, a gas phase reaction control method, a regenerant purification control method, a catalyst delivery pipeline
  • the regenerant purification control method includes catalyst temperature control and carrier gas control, and also includes a regenerant purification controller, a catalyst control method, a control medium, a temperature detection, and an adjustment control.
  • the catalyst control and regenerant heat removal control method of the invention consists of the following steps:
  • the regenerated catalyst enters the reactor in three ways, and the regenerated catalyst from the regenerator directly enters the bottom of the reactor through the regeneration riser, and the other regenerant reaches the required temperature in the purification controller, After replacing the carried gaseous medium, one or two transfer pipes are introduced into the reactor: in the first transfer pipe, the catalyst enters below the reaction raw material entry point by gravity, and is mixed with the regenerant from the regeneration riser to lower the reactor.
  • the temperature of the internal regenerant adjusts the amount of catalyst from the regenerant purification controller to control the temperature of the catalyst before the regenerant and the feedstock are contacted, and increases the ratio of the agent to the oil; in the second transfer pipe, the catalyst enters the feedstock feed by gravity downward a gas phase reaction zone above the point; 2.
  • the catalyst temperature in the regenerant purification controller is controlled according to the temperature of the gas phase reaction zone above the feed point of the reactor reaction raw material, so that the catalyst entering the gas phase reaction zone is adapted to the reaction conditions of the gas phase reaction zone.
  • a temperature measurement point generally a thermocouple
  • a temperature measurement point is provided at a reaction zone between the catalyst entry point of the reactor gas phase reaction zone and the reaction material entry point, and is generally a thermocouple, and the difference between the two temperatures is used.
  • the indicator controls the regenerant purification controller to operate the medium line to adjust the opening degree, or the temperature difference between the reactor outlet and the regenerant purification controller is used as an index to control the regenerant purification controller to operate the medium line to adjust the opening degree; Further controlling the amount of operating medium entering the regenerator purification controller to achieve associated control of the catalyst and reactor reaction temperatures in the regenerant purification controller, so that the catalyst entering the gas phase reaction zone of the reactor is always adapted to the conditions in the reactor;
  • the temperature of the regenerant purification controller is used as an index to control the operation medium of the regenerant purification controller to adjust the opening degree, adjust the amount of the incoming fluidized medium, and realize the control of the temperature of the regenerant purification controller;
  • a catalyst temperature measurement point is generally set below the feed point of the reactor raw material, generally a thermocouple, which controls the slip opening of the first transfer tube of the regenerant purification controller, and adjusts the amount of catalyst entering the reactor from the regenerator purification controller. Controlling the amount of catalyst entering the reactor gas phase reaction zone from the regenerator purge controller by the slip opening on the second transfer pipe;
  • the regenerant purification controller of the invention uses steam as an operation medium, realizes replacement of the regenerator carrying flue gas by steam, or sets two operating media of air and steam, and the steam enters the regenerant purification controller under the air; Changing the catalyst temperature; adjusting the amount of steam controls the catalyst temperature and the gas composition carried.
  • the catalyst of the regenerant purification controller of the present invention enters the gas phase reaction zone from a space of a reaction time of 0.1 second to 1.0 second from the second transfer pipe at the entry point of the reaction raw material; or 1.0 to 10 m above the entry point of the reaction raw material
  • the zone enters the reactor gas phase reaction zone.
  • the regenerator purification controller of the present invention is provided with a heat exchange tube, and while the regenerant is cooled, the reaction raw material is heated in the heat exchange tube and then enters the reactor; or steam is generated in the heat exchange tube.
  • the reaction raw material of the present invention is added with water which does not exceed 20% by weight of the heated raw material before being heated into the heat exchange tube of the regenerant purification controller; and then enters the reactor after heating.
  • the regenerator thermal cooling method of the present invention comprises a regenerant purification control section, a carrier gas displacement control, a catalyst temperature control, a steam regulation and a stripping gas discharge line, and a regenerated catalyst inlet and outlet line section; the regenerated catalyst enters through an inlet pipe, through a Or two pipes are discharged and sent to the reactor, steam enters in the bottom area of the regenerant purification controller, the stripping gas and the regenerant carrier gas are discharged at the upper portion, and the steam enters the pipeline to set the regulation ⁇ , which is controlled by the regenerant purification Catalyst temperature control or purification of the regenerative agent from the corresponding location of the reaction zone The controller's catalyst temperature difference is controlled.
  • a catalyst-carrying gas stripper is disposed, and the stripper is disposed below the heat exchange tube.
  • the reactor gas phase reaction zone of the reaction regenerant control method of the present invention is provided with a catalyst mixing partition at a point where the catalyst is cooled, the mixing section having a larger diameter than the reactor.
  • the reactor gas phase reaction zone of the present invention is a riser reactor, or a reaction section in which the catalyst is introduced into the mixed distribution section; the gas phase flow rate in the section is from 1. 8 m/s to 4.0 m/s, and the reaction time is 3.0 seconds. To 5. 5 seconds.
  • the present invention also provides an apparatus for implementing the reaction zone catalyst control and regenerant purification and heat removal method, the apparatus comprising a regenerator, an external heat extractor, a regenerant purification controller, and a reactor, wherein:
  • the regenerator is connected to the external heat extractor and is also connected to the regenerant purification controller.
  • the regenerant purification controller is connected to the reactor through two conveying pipes, and the regenerator purifying controller bottom leads the first conveying pipe to the catalyst mixing.
  • the riser, the lower part of the regenerant purification controller leads the second delivery pipe to the catalyst distributor connection port located above the reactor feed nozzle
  • the reactor of the present invention is a riser reactor, and the gas phase reaction zone of the riser reactor may be provided with an expanded diameter reaction zone.
  • the regenerated catalyst from the regenerator enters the reactor through the regeneration riser below the feed nozzle, and after the completion of the reaction, is stripped back to the regenerator via the stripping section; another part of the catalyst from the regenerator is processed into the reactor by the regenerant purification controller;
  • the temperature of the cooled catalyst is controlled according to the difference between the temperature of the temperature measurement point set in the gas phase reaction zone of the reactor or the temperature of the temperature measurement point set in the gas phase reaction zone of the reactor, or the temperature of the catalyst after the heat recovery of the regenerated catalyst is determined according to the reactor.
  • the difference between the outlet temperature or the outlet temperature of the reactor is controlled; the catalyst in the regenerant purification controller is then steam stripped to remove the carried oxygen and other gases, and then sent to different parts of the reactor by gravity through two tubes. After the reaction is completed, it is stripped back to the regenerator; the steam enters the regenerant purification controller at the bottom of the regenerant purification controller, passes upward through the stripping zone and the cooling zone, and is discharged at the top exhaust line;
  • the temperature of the catalyst below the reactor feed point is controlled by the regenerator purification controller first transfer tube; the reaction temperature between the reactor feed point and the gas phase reaction zone is controlled by the regeneration riser slip, and the reactor outlet temperature is controlled by The second delivery pipe slide valve is controlled by controlling the amount of catalyst entering from the regenerant purification controller; or the reactor outlet temperature is controlled by the regeneration riser slip; the regenerant purification controller catalyst temperature is set by the temperature with the reactor set point Difference Control the amount of gas entering by adjusting ⁇ .
  • the invention has the following beneficial effects:
  • the present invention can conveniently supplement the gas-phase reaction zone with a high activity, consistent with the reaction temperature, and remove the carrier-carrying catalyst; increase the activity of the gas-phase reaction zone catalyst and the reactant oil.
  • the present invention can control the catalyst to enter the reactor without affecting the heat balance of the reaction by controlling the temperature of the catalyst after the hot reheating by the reactor reaction temperature, and can freely increase the ratio of the catalyst to the oil in the gas phase reaction zone; Restricted by the density of the reaction raw materials and the boiling point;
  • the catalyst of the method of the invention enters the reaction zone to be purified, and the oxygen, nitrogen and gas from the regenerator are replaced, which avoids the influence of these gases on the reaction, reduces the pressure of the air compressor, and reduces the energy consumption;
  • the invention realizes that the catalyst after the regenerator is cooled by heat directly enters the reactor by gravity, does not need to transport the medium, does not increase other influences on the reaction except the catalyst, and has low energy consumption;
  • the present invention uses a regenerant purification controller to achieve multiple control of the reaction catalyst.
  • Fig. 1 is a schematic view showing the process flow of a reaction zone catalyst control and regenerant heat removal method of the present invention.
  • Fig. 2 is a schematic view showing the process flow of another reaction zone catalyst control and regenerant heat removal method of the present invention.
  • Fig. 3 is a schematic view showing the process flow of another reaction zone catalyst control and regenerant heat removal method of the present invention.
  • Figure 4 Schematic diagram of the apparatus for the reaction zone catalyst control and regenerant heat removal of the present invention.
  • FIG. 5 Example 1 Schematic diagram of the apparatus for the reaction zone catalyst control and regenerant heat removal method.
  • Figure 6 Example 2 Scheme of catalyst for catalyst control and regenerant heat removal.
  • Figure 7 is a schematic view showing the process flow of Embodiment 1 of the present invention.
  • Figure 8 is a schematic view showing the process flow of Embodiment 2 of the present invention.
  • the numbering in the figure shows: I reactor raw material and catalyst contact gasification zone; II reactor gas phase reaction zone; ⁇ expansion reaction section; 1 regenerator; 2 regenerant purification controller; 3 reactor; 11 regenerator transition section; 12 regenerator scorch tank; 13 external heat extractor; 14 external heat extractor; 15 external heat extractor; 21, 22 expansion joint; 23, 24 regenerant purification controller catalyst delivery tube; 26 regenerant purification controller catalyst delivery pipe slip; 27 regenerant purification controller stripping zone; 28 regenerant purification controller cooling zone; 29 regenerant purification controller top exhaust pipe; 30 catalyst mixing riser; Feed nozzle; 32 catalyst distributor; 33 regeneration riser; 34 standby riser; 35 stripping section; 36 cyclone; 37 settler; 38 regenerative slip; 40 compressed air; 41 water; 42 water, steam Mixture; 43 steam or air; 44, 46, 47, 48 steam; 45 atomizing steam; 49 quenching medium; 50 supercharged air self-pressurizer; Pre-lifting medium; 52 feedstock oil; 53 refining oil; 54, 58 accident bypass line
  • the invention provides a reaction zone catalyst control and a regenerant purification and heat removal cooling method, which is mainly used for a catalytic reaction process of a petroleum hydrocarbon raw material or an alcohol raw material; the method comprises the control of the reaction and the control of the catalyst entering the reactor, and the method
  • the apparatus used includes the following parts: reactor, catalyst regenerator, regenerant purification controller, catalyst delivery pipeline; control of reaction including liquid phase contact gasification reaction control, gas phase reaction process control, reactor outlet temperature control;
  • the control of the catalyst entering the reactor includes regenerant temperature control and purification control of the catalyst-carrying gas entering the reactor; the regenerant enters the purification controller and is cooled by the heat exchange tube to control the temperature, while replacing the carried gas with steam, including nitrogen.
  • the catalyst flows downward from the catalyst delivery tube into the reactor under the reaction feed entry point or / and the reaction feedstock and catalyst contact vaporization zone, so that the reactor is Pre-reaction, liquid phase gas
  • the regenerated catalyst in the method for controlling the catalyst of the reactor, can be divided into three steps into the reactor, and one regenerative catalyst from the regenerator directly enters the bottom of the reactor through the regeneration riser, and the other regenerant is cooled in the purification controller.
  • the two transfer pipes After controlling the temperature to the required temperature and replacing the gaseous medium carried by the regenerant, the two transfer pipes enter the reactor, and the two transfer pipes are provided with a catalyst flow control trick: from the regenerator purification controller in the first transfer pipe
  • the catalyst enters below the reaction feed point by gravity, mixes with the regenerant from the regeneration riser, reduces the temperature of the regenerant in the reactor, and regulates the amount of catalyst from the regenerant purification controller to control the contact of the regenerant and the feedstock.
  • the former temperature the ratio of the agent to the oil
  • the catalyst after the purification in the second transfer pipe, the catalyst enters the gas phase reaction zone above the feed point of the reaction raw material by gravity; the catalyst temperature measurement point is set below the feed point of the reactor raw material, the temperature Controlling the opening of the first delivery tube of the regenerant purification controller to regulate the catalysis entering the reactor Amount; Min door opening degree control on the amount of second pipes to the catalyst reactor gas phase reaction zone.
  • the regenerant purification and heat removal includes a regenerant purification control portion, a carrier gas stripping, a catalyst temperature control, a steam adjustment and a stripping gas discharge line, and a regenerated catalyst inlet and outlet line portion; the regenerated catalyst enters through an inlet pipe, One or two transfer pipes are discharged and sent to the reactor, steam enters in the bottom region, the stripping medium and the regenerant carry gas are discharged at the upper portion, and the steam enters the pipeline to set a regulating enthalpy, which adjusts the catalyst of the regenerant purification controller
  • the temperature control is either controlled by the temperature of the corresponding location in the reaction zone and the catalyst temperature difference of the regenerant purge controller.
  • the catalyst temperature in the regenerant purification controller is controlled according to the temperature of the gas phase reaction zone above the feed point of the reactor, so that the catalyst entering the gas phase reaction zone is adapted to the reaction conditions of the gas phase reaction zone;
  • the reaction zone between the catalyst entry point and the reaction raw material entry point and the regenerant purification controller set the temperature measurement point, and the two temperature differences are used as indicators to control the regenerant purification controller to operate the medium pipeline to be opened.
  • the regulating valve further controls the amount of operating medium entering the regenerant purification controller, Correlation control of the catalyst and reactor reaction temperature in the regenerant purification controller, so that the catalyst entering the gas phase reaction zone of the reactor is always adapted to the conditions in the reactor; or the temperature of the regenerant purification controller is used as an index to control the regenerator
  • the purification controller operates the medium line to adjust the opening degree, The amount of fluidizing medium that is introduced is adjusted to achieve control of the temperature of the regenerant purification controller.
  • the regenerant purification controller of the invention uses steam as an operation medium, realizes replacement of the regenerator carrying flue gas and control of the catalyst temperature by steam; or sets two operating media of air and steam, and the steam enters the regenerant purification control under the air. Adjusting the amount of air can change the catalyst temperature; adjusting the amount of steam can control the catalyst temperature and the displacement effect of the carrier gas.
  • the catalyst of the regenerant purification controller of the present invention enters the reactor gas phase reaction zone from the space of the reaction time of the second transfer pipe from the entry point of the reaction raw material from 0.1 second to 1.0 second; or above the reaction raw material entry point 1.0
  • the reactor gas phase reaction zone is entered in the area of meters to 10 meters.
  • the regenerator purification controller of the present invention is provided with a heat exchange tube in the upper part of the controller, and while the regenerant is cooled, the reaction raw material is heated in the heat exchange tube and then enters the reactor; or steam is generated in the heat exchange tube;
  • the catalyst is provided with a gas replacement zone.
  • the reaction raw material of the present invention is added with water which does not exceed 20% by weight of the heated raw material before being heated into the heat exchange tube of the regenerant purification controller; and then enters the reactor after heating.
  • the reactor gas phase reaction zone of the reaction regenerant control method of the present invention is provided with a catalyst mixing distribution section at the inlet of the cooling purification catalyst, the mixed distribution section having a larger diameter than the reactor.
  • the reactor gas phase reaction zone of the present invention is a riser reactor, or a reaction section having an expanded diameter above the mixed distribution section of the cooling purification catalyst; the gas phase flow rate in the expanded section is 1. 8 m/s to 4.0 m/s, The reaction time is from 3.0 seconds to 5.5 seconds.
  • FIG. 1 is a schematic view showing the process flow of a reaction zone catalyst control and regenerant purification and heat removal method of the present invention.
  • the regenerated catalyst enters the reactor 3 in three ways, and the regenerated catalyst from the regenerator 1 directly enters the catalyst mixing riser 30 at the bottom of the reactor 3 via the regeneration riser 33, and after the reaction is completed, the carried oil and gas is stripped in the stripping section 35,
  • the standby riser 34 is returned to the regenerator scorch tank 12 (the riser 34 and the regenerator scorch tank 12 are not shown in FIG. 1, please refer to FIG. 4 together), and the other catalysts from the regenerator 1 are regenerated.
  • the agent purification controller 2 After the agent purification controller 2 processes, it is sent to the reactor 3 under the action of gravity through two transfer tubes (the regenerant purification controller catalyst delivery tubes 23, 24), and after the reaction is completed, the carried oil and gas is stripped in the stripping section 35, Returning to the regenerator scorch tank 12 via the standby tube 34: in the first delivery tube (the regenerant purification controller catalyst delivery tube 24), the catalyst flows downward by gravity into the catalyst mixing riser 30 below the reaction material entry point, and The regenerant is mixed by the regeneration riser 33; the first conveying pipe is adjusted according to the reaction temperature below the feed point of the reactor raw material (catalyst mixing pre-lifting section temperature measuring point 83) The slide of the purification controller catalyst delivery pipe 24) (regeneration agent purification controller catalyst delivery pipe slip 26) opening degree, controlling the catalyst intake amount from the regenerant purification controller 2; in the second delivery pipe (regenerative purification control) In the catalyst delivery tube 23), the catalyst enters the reactor gas phase reaction zone II above the feedstock feed point by gravity, according to
  • FIG. 2 is a schematic view showing the process flow of another reaction zone catalyst control and regenerant purification and heat removal method of the present invention.
  • the regenerated catalyst enters the reactor 3 in three ways, and the regenerated catalyst from the regenerator 1 directly enters the catalyst mixing riser 30 at the bottom of the reactor 3 through the regeneration riser 33, and after the reaction is completed, the carried oil and gas is stripped in the stripping section 35,
  • the standby riser 34 is returned to the regenerator scorch tank 12 (the riser 34 and the regenerator scorch tank 12 are not shown in FIG. 1, please refer to FIG. 4 together), and the other catalysts from the regenerator 1 are regenerated.
  • Two transfer tubes (regenerant purification controller catalyst delivery tubes 23, 24) are fed into the reactor 3 by gravity, and after completion of the reaction, are returned to the regenerator scorch tank 12 via the stripping section 35: in the first transfer tube (regeneration)
  • the catalyst purification controller catalyst delivery pipe 24) is charged downward by gravity into the catalyst mixing riser 30 below the reaction raw material entry point, and is mixed with the regenerant via the regeneration riser 33; according to the reaction temperature below the feed point of the reactor raw material (catalyst mixing pre-lifting section temperature measuring point 83), adjusting the sliding degree of the first conveying pipe (regenerant cleaning controller catalyst conveying pipe 24) (regeneration agent purification controller catalyst conveying pipe sliding 26), the control comes from The amount of catalyst entering the regenerant purification controller 2; in the second delivery pipe (regeneration agent purification controller catalyst delivery pipe 23), the catalyst flows downward by gravity into the reactor gas phase reaction zone II above the feedstock feed point, according to the reaction 3 outlet reaction temperature temperature measuring point 85 and regenerant purification
  • Fig. 3 is a schematic illustration of the process flow of another reaction zone catalyst control and regenerant purification and heat removal method of the present invention.
  • the regenerant takes the heat controller 2 and sends the compressed air 40; the reaction raw material (the mixed oil of the raw material oil and the refinery oil 59) is heated in the heat exchange tube of the regenerant purification controller 2, and then passed through the feed nozzle 31. Entering reactor 3; otherwise the same as in Example 2.
  • Fig. 4 is a schematic view showing a device for controlling a catalyst in a reaction zone and a method for purifying and purifying a heat of the regenerator according to the present invention.
  • the regenerator 1 is connected to the external heat extractor 13, and is also connected to the regenerant purification controller 2, and the regenerant purification controller 2 is reacted via two transfer tubes (regeneration agent purification controller catalyst delivery tubes 23, 24)
  • the third phase of the regenerant purification controller 2 leads to the first delivery tube (the regenerant purification controller catalyst delivery tube 24) to the catalyst mixing riser 30, and the lower portion of the regenerant purification controller 2 leads the second delivery tube (regeneration)
  • the reagent purification controller catalyst delivery tube 23) is connected to the catalyst distributor 32 at a port above the reactor feed nozzle 31.
  • the gas phase reaction zone of the riser reactor is provided with an expanded diameter reaction section III (expanded reaction zone).
  • a petroleum hydrocarbon catalytic cracking unit with an annual output of 100 X 10 4 t/a is regenerated by scorch tank, and the reaction regeneration is arranged side by side.
  • the riser reactor 3, the regenerant purification controller 2 generates medium pressure steam, and the regenerant purification controller 2
  • the self-contained vapor-liquid separator type is adopted, and the gas-liquid separator is directly connected to the regenerant purification controller 2, and the diameter is the same as the purification controller.
  • Reheating agent purification controller 2 heat exchange tube area m 2 90
  • Example comparative example A petroleum hydrocarbon catalytic cracking unit with an annual output of 100 X 10 4 t/a is regenerated by scorch tank, and the reaction regeneration is arranged side by side.
  • the riser reactor 3 is provided.
  • the expanded diameter reaction zone III is set above the gas phase reaction zone II.
  • Other conditions and implementation Example 1 is the same.
  • the reaction materials and the comparative conditions of Example 2 and the prior art are shown in the following table.

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Abstract

一种用于石油烃类原料或醇类原料催化反应过程的反应区催化剂控制和再生剂净化取热冷却方法及装置，所述装置包括催化剂再生器、外取热器、再生剂净化控制器、反应器、催化剂输送管道，其中再生器与外取热器和再生剂净化控制器相连接，再生剂净化控制器经两个输送管与反应器相连接。所述方法包括对反应的控制和对参与反应的催化剂的控制，有以下部分：原料液相接触气化反应控制，气相反应控制；再生剂先经过净化控制器出来，脱除携带的氮气、氧气、二氧化碳和杂质气体，控制温度达到反应要求后分别进入反应器原料进入点下方和气化接触区上方，使反应器实现对反应前、液相气化反应后和反应器出口反应条件的三级控制，同时限制再生剂携带的氮气和氧气进入反应器，提高产品收率。

Description

一种反应区催化剂控制和再生剂净化取热冷却方法及装置 技术领域
本发明涉及一种石油和化工领域催化反应技术，特别是涉及一种用于催化反应中催 化剂的控制和再生催化剂 （再生剂） 降温、 净化方法， 并涉及实现该方法的反应区催化 剂控制和再生剂净化取热冷却装置。 背景技术
在催化反应过程中， 催化剂是核心问题， 但反应过程中催化剂的性能和未反应前催 化剂的性能是不同的。 以烃类或醇类化合物原料反应为例， 反应过程中催化剂会出现结 焦、 碱性成分和金属污染、 钝化， 使实际反应过程中催化剂的性能远低于未反应前的性 能。 反应过程中催化剂的活性、 反应剂油比或空速、 反应原料和催化剂的温度及温度差 等反应条件都是影响反应结果的重要因素。
在催化反应过程中反应条件的选择和控制直接关系到反应转化率和反应选择性。现 行优化反应系统操作的技术很多， 以催化转化反应为例， 干气预提升技术、 采用改变原 料注入点和注入介质的混合温度控制技术、 出口区快速分离技术、 急冷终止技术等都对 反应结果影响明显， 已在工业上得到较好应用。 反应过程中催化剂性能的改进和控制也 是至关重要的。 许多气固反应过程需要固相物如催化剂冷却， 使反应条件改善后进行， 尤其对例如催化转化反应的气固反应过程， 把再生催化剂适当降温可以提高剂油比， 抑 制热裂化反应， 改进产品分布。
以石油烃类原料催化转化为例， 国内外的研究结果早就证实， 再生剂温度高， 导致 反应剂油比较低， 与反应原料间的接触温差大， 都会导致干气产率高， 对收率产生显著 影响；提升管内随着反应的进行，催化剂的活性快速降低，提升管下游反应区效率降低， 影响反应效果。 降低再生剂温度， 提高剂油比和提高提升管内催化剂的活性是多年来催 化裂化装置一直追求的目标。
使用管式反应器的液体原料催化反应都存在液相气化接触反应和气相反应两个反 应区域。 液相气化反应区催化剂和原料间的温差和催化剂的高温都会增加热裂化反应， 增加 C2以下副产品比例， 影响经济效益。
在降低反应原料液相气化接触反应区的再生剂和原料油温差方面有不少技术措施。 针对降低与原料油起始接触温度问题， 最容易想到的办法是 "把外取热器内的低温催化 剂引入提升管预提升段"。 UOP公司于上世纪 90年代在专利 US5800697中提出了把外 取热器内的低温催化剂送入提升管提预提升段的方法。 这方面的专利申请较多， 如 US6059958, US6558530B1，中国专利申请 01119805.1， 200510055695.4， 200710054738.1 , 200710054739.0等。
专利 US5800697公开了一种催化转化反应 -再生方法， 在再生器旁边设置催化剂降 温区， 来自密相床的热再生剂从出口进入降温区换热至适宜温度后经再生立管、 滑闽进 入提升管反应器底部参与反应， 从而使反应温度成为独立变量。 中国专利 200610113673.3公开了一种石油烃类的转化方法，热的再生催化剂通过冷却器冷却返回 到反应器底部与原料油接触并进行裂化反应，待生催化剂经汽提后输送到再生器进行烧 焦再生后循环使用或部分直接进入反应器底部的混合器。中国专利 200710054738.6公开 了一种催化裂化装置的再生催化剂调温设备， 在再生器密相床的旁边设置催化剂降温 器， 催化剂降温器内设有换热管， 上部设有烟气返回管线， 沿催化剂降温器垂直高度分 段设置流化环， 经降温的再生催化剂进入提升管反应器预提升段参与反应。 中国专利 200710054737.1也公开了一种催化裂化装置再生催化剂调温设备，在再生器密相床内设 置一隔板， 将再生器密相床分成两个区， 一个区为再生烧焦区， 另一个区为催化剂降温 区， 隔板下部设有降温器催化剂入口， 催化剂降温区内设有换热管， 经降温的再生催化 剂进入提升管反应器预提升器参与反应。
另一种降低原料油和再生剂起始接触温差的办法是把原料油的温度提高。中国专利 200610127585.9公开了一种烃油裂化方法， 将烃油与再生催化剂在换热器中加热， 然后 使换热后的烃油与换热后的再生催化剂在反应器中接触反应。
已有对反应条件的优化控制技术， 主要集中在反应原料流程优化， 反应温度、 时间 优化方面， 对反应过程中催化剂性能控制优化关注较少。 以上公开的专利文献， 也仅仅 涉及降低预提升段再生剂的温度。
在以上降低再生剂温度的专利文献中来自外取热器的催化剂携带一定氧气和再生 烟气， 这部分氧气进入了反应器与反应介质发生反应， 存在着进入反应器的氧气会影响 产品的问题； 而来自再生催化剂携带的烟气会加大富气压机负荷， 增加能耗。
另外， 反应催化剂控制不仅包括反应前的催化剂温度、 液相气化反应区接触温差和 剂油比， 气相反应区催化剂活性和剂油比的控制对反应效果也有重要影响。
现有提升管反应器出口处的催化剂活性只有初始活性的 1/3左右， 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 次反应比例增加。 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 力口。 控制提升管反应器后半段的催化剂活性是重要问题。 CN99213769. 1公开了一种用 于催化裂化的两段串联式提升管反应器， 该反应器由两提升管头尾相接串联而成， 该技 术通过采用两段接力式的反应装置， 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。 但该技术限于原理， 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装置， 投资费用高， 实施可能性很小。
对反应过程中催化剂的控制， 除对液相气化反应区外， 还应包括对气相反应区的催 化剂控制、 对提供的催化剂状态的控制、 以及对催化剂携带气体的控制。
再者， 在向反应器气相反应区补充催化剂时， 对进入反应器的催化剂温度控制也是 至关重要的。 此部分催化剂会影响反应的热平衡， 不仅对反应出口温度有影响， 也对接 触气化区有影响。 只有催化剂温度和反应要求相适应， 才能改进反应。
综上， 对进入反应器的催化剂的控制有重要意义。 发明内容
本发明的主要目的在于提供一种反应区催化剂控制和再生剂净化取热冷却方法， 实 现方便灵活地对反应区催化剂进行多处控制， 且降低能耗。
本发明的另一目的在于提供一种用于实现上述方法的装置。
为达上述目的， 本发明提供了一种反应区催化剂控制和再生剂取热冷却方法， 用于 石油烃类原料或醇类原料催化反应过程。该方法包括对反应的控制和对参与反应的催化 剂的控制， 有以下部分： 反应器， 催化剂再生器， 液相接触气化反应控制方法， 气相反 应控制方法， 再生剂净化控制方法， 催化剂输送管道； 再生剂净化控制方法包括催化剂 温度控制和携带气体控制， 还包括再生剂净化控制器， 催化剂控制方法， 控制介质， 温 度检测， 调节控制闽。 该发明的催化剂控制和再生剂取热冷取控制方法由以下几个环节 组成：
1、 本发明的再生剂净化控制方法中， 再生催化剂分三路进入反应器， 来自再生器 的再生催化剂经再生立管直接进入反应器底部，其他再生剂在净化控制器内达到要求的 温度、 置换携带的气体介质后， 分一个或两个输送管进入反应器： 在第一输送管中催化 剂靠重力向下进入反应原料进入点下方， 与经再生立管来的再生剂混合， 降低反应器内 再生剂的温度，调节来自再生剂净化控制器的催化剂量来控制再生剂和原料油接触前的 催化剂温度， 提高剂油比； 在第二输送管中催化剂靠重力向下进入原料油进料点上方的 气相反应区； 2、 根据反应器反应原料进料点上方的气相反应区温度对再生剂净化控制器内催化 剂温度进行控制， 使进入气相反应区的催化剂与气相反应区反应条件相适应。 为实现该 发明要求， 分别在反应器气相反应区催化剂进入点和反应原料进入点之间的反应区及再 生剂净化控制器处设置测温点， 一般为热电偶， 由该两处温度差作为指标， 控制再生剂 净化控制器操作介质管线调节闽开度， 或者由反应器出口和再生剂净化控制器的温度差 作为指标， 控制再生剂净化控制器操作介质管线调节闽开度； 该调节闽进一步控制进入 再生器净化控制器的操作介质量， 实现对再生剂净化控制器内催化剂和反应器反应温度 的关联控制， 使进入反应器气相反应区的催化剂始终适应反应器内的条件； 或者用再生 剂净化控制器的温度作为指标控制进入该再生剂净化控制器操作介质管线调节闽开度， 调节进入的流化介质量， 实现对再生剂净化控制器的温度的控制；
3、 控制经再生剂净化控制器进入反应器的催化剂量。 在反应器原料进料点以下设 置催化剂测温点，一般为热电偶，该温度控制再生剂净化控制器第一输送管的滑闽开度， 调节从再生器净化控制器进入反应器的催化剂量； 用第二输送管上的滑闽开度控制从再 生器净化控制器进入反应器气相反应区的催化剂量；
4、 控制经再生剂净化控制器进入反应器的催化剂携带的氧气及再生催化剂携带的 烟气量。 本发明的再生剂净化控制器用蒸汽作为操作介质， 用蒸汽实现对再生剂携带烟 气的置换；或者设置空气和蒸汽两种操作介质，蒸汽在空气下方进入再生剂净化控制器; 调节空气量可以改变催化剂温度； 调节蒸汽量可以控制催化剂温度和携带的气体成分。
本发明的再生剂净化控制器的催化剂从第二输送管在反应原料进入点起上方 0.1秒 至 1.0秒的反应时间的空间内进入气相反应区； 或者在反应原料进入点以上 1.0米至 10 米的区域内进入反应器气相反应区。
本发明再生剂净化控制器内设置换热管， 在冷却再生剂的同时， 反应原料在该换热 管内加热， 然后进入反应器； 或者在换热管内发生蒸汽。
本发明的反应原料在进入再生剂净化控制器换热管加热前加入占被加热原料重量 不大于 20%的水； 加热后再进入反应器。
本发明的再生剂取热冷却方法包括再生剂净化控制部分、 携带气体置换控制、 催化 剂温度控制、 蒸汽调节和汽提气排出管线、 再生催化剂进出管线部分； 再生催化剂经一 个入口管进入， 经一个或两个输送管排出并送入反应器， 蒸汽在再生剂净化控制器底部 区域进入， 汽提气体和再生剂携带气体在上部排出， 蒸汽进入管线设置调节闽， 该调节 闽由再生剂净化控制器的催化剂温度控制或者由反应区相应位置的温度与再生剂净化 控制器的催化剂温度差控制。
本发明的反应区催化剂控制和再生剂取热冷却方法的再生剂净化控制器内除设置 换热管外还设置催化剂携带气体汽提器， 汽提器设置在换热管下方。
本发明的反应再生剂控制方法的反应器气相反应区在冷却催化剂进入处设置催化 剂混合分配段， 该混合分配段直径大于该处反应器。
本发明的反应器气相反应区为提升管反应器， 或在催化剂进入混合分配段上方设置 扩径的反应段； 该段内气相流速 1. 8m/s至 4. 0m/s， 反应时间 3.0秒至 5. 5秒。
本发明还提供了一种用于实现所述反应区催化剂控制和再生剂净化取热冷却方法 的装置， 该装置包括再生器、 外取热器、 再生剂净化控制器、 反应器， 其中：
再生器与外取热器相连接， 还与再生剂净化控制器相连接， 再生剂净化控制器经两 个输送管与反应器相连接， 再生剂净化控制器底部引出第一输送管到催化剂混合提升 器， 再生剂净化控制器中下部引出第二输送管到位于反应器进料喷嘴的上方的催化剂分 配器连接口
根据本发明的具体实施方案， 本发明中的反应器为提升管反应器， 提升管反应器气 相反应区可以设置扩径反应区。
本发明的具体的用于实现所述反应区催化剂控制和再生剂净化取热冷却方法的装 置可参见图 1〜图 8所示。
本发明的任务是这样实现的：
来自再生器的再生催化剂经再生立管在进料喷嘴下方进入反应器， 完成反应后经汽 提段汽提返回再生器； 另一部分来自再生器的催化剂经再生剂净化控制器处理进入反应 器； 冷却后的催化剂温度根据反应器气相反应区设定测温点的温度或与反应器气相反应 区设定测温点温度的差控制， 或再生催化剂经取热冷却后的催化剂温度根据反应器的出 口温度或与反应器出口温度的差控制； 再生剂净化控制器内的催化剂再经过蒸汽汽提除 去携带的氧气和其他气体， 然后经两个输送管在重力作用下送入反应器不同部位， 完成 反应后经汽提返回再生器； 蒸汽在再生剂净化控制器底部进入再生剂净化控制器， 向上 经过汽提区和冷却区， 在顶部排气管线排出；
反应器原料进入点下方的催化剂温度由再生剂净化控制器第一输送管滑闽控制； 反 应器原料进入点和气相反应区之间的反应温度由再生立管滑闽控制， 反应器出口温度由 第二输送管滑阀通过控制从再生剂净化控制器进入的催化剂量来控制； 或者反应器出口 温度由再生立管滑闽控制； 再生剂净化控制器催化剂温度由与反应器设定点的温度的差 通过调节闽调节进入的气体量控制。
本发明与现有技术相比， 其有益效果是：
首先， 除向反应器进料下方补充低温再生剂外， 本发明可以方便的向气相反应区补 充高活性、 与反应温度一致、 除去携带气体的催化剂； 增加气相反应区催化剂的活性和 反应剂油比；
第二， 本发明通过由反应器反应温度控制再生剂取热冷却后的催化剂温度的方法， 使进入反应器的催化剂不影响反应的热平衡，可以自由地增加气相反应区的催化剂剂油 比； 不受反应原料密度大小、 沸点高低的限制；
第三， 本发明的方法进入反应区的催化剂得到净化， 置换出了携带的氧气、 氮气和 来自再生器的气体， 避免了这些气体对反应的影响， 降低了气压机负荷， 降低能耗； 第四， 本发明实现了再生剂取热冷却后的催化剂直接靠重力进入反应器， 不需要输 送介质， 除催化剂外不增加对反应的其他影响， 能耗低；
第五， 本发明用一台再生剂净化控制器实现对反应催化剂的多处控制。 附图说明
图 1 : 本发明的一种反应区催化剂控制和再生剂取热冷却方法的工艺流程示意图。 图 2:本发明的另一种反应区催化剂控制和再生剂取热冷却方法的工艺流程示意图。 图 3:本发明的另一种反应区催化剂控制和再生剂取热冷却方法的工艺流程示意图。 图 4: 本发明的反应区催化剂控制和再生剂取热冷却方法的装置示意图。
图 5: 实施例 1反应区催化剂控制和再生剂取热冷却方法的装置示意图。
图 6: 实施例 2反应区催化剂控制和再生剂取热冷却方法的装置示意图。
图 7: 本发明实施例 1的工艺流程示意图。
图 8: 本发明实施例 2的工艺流程示意图。
图中编号说明： I反应器原料和催化剂接触气化区； II反应器气相反应区； ΙΠ扩径 反应段； 1再生器； 2再生剂净化控制器； 3反应器； 11再生器过渡段； 12再生器烧焦 罐； 13外取热器； 14外取热器滑闽； 15外取热器烟气管； 21,22膨胀节； 23,24再生剂 净化控制器催化剂输送管； 25,26再生剂净化控制器催化剂输送管滑闽； 27再生剂净化 控制器汽提区； 28再生剂净化控制器冷却区； 29再生剂净化控制器顶部排气管； 30催 化剂混合提升器； 31进料喷嘴； 32催化剂分配器； 33再生立管； 34待生立管； 35汽提 段； 36旋分器； 37沉降器； 38再生滑闽； 40压缩空气； 41进水； 42水、 蒸气混合物； 43蒸汽或空气； 44,46,47,48蒸汽； 45雾化蒸汽； 49急冷介质； 50增压风自增压机； 51 预提升介质； 52原料油； 53回炼油； 54,58事故旁通线； 55反应原料 2 ； 56油浆； 57 原料油回炼油混合器； 59原料油与回炼油的混合油； 80再生剂净化控制器催化剂温度 测温点； 81净化控制器与气相反应区补剂测温点的温度之差； 83催化剂混合预提升段 温度测温点； 84原气相反应区补剂测温点； 85反应器出口反应温度测温点； 90进再生 剂净化控制器蒸汽或空气的调节闽； 91进再生剂净化控制器蒸汽的调节闽； 92进再生 剂净化控制器压缩空气的调节闽。 具体实施方式
以下结合附图及实施例详细说明本发明的技术方案，但本发明的保护范围包括但是 不限于此。
本发明提供的反应区催化剂控制和再生剂净化取热冷却方法， 主要用于石油烃类原 料或醇类原料催化反应过程； 该方法包括对反应的控制和对进入反应器的催化剂的控 制， 方法中所用装置包括有以下部分： 反应器， 催化剂再生器， 再生剂净化控制器， 催 化剂输送管道； 对反应的控制包括液相接触气化反应控制， 气相反应过程控制， 反应器 出口温度控制； 对进入反应器的催化剂的控制包括再生剂温度控制和进入反应器的催化 剂携带气体的净化控制； 再生剂进入净化控制器后被换热管冷却控制温度， 同时用蒸汽 置换出携带的气体， 包括氮气、 二氧化碳和氧气， 达到要求的温度和气体携带要求后的 催化剂从催化剂输送管靠重力向下进入反应器反应原料进入点下方或 /和反应原料和催 化剂接触气化区上方， 使反应器实现对反应前、 液相气化反应后和反应出口反应条件的 多级控制， 同时限制再生剂携带的氮气、 氧气和二氧化碳进入反应器。
本发明中， 对反应器的催化剂的控制方法中， 再生催化剂可分三路进入反应器， 一 路来自再生器的再生催化剂经再生立管直接进入反应器底部，其他再生剂在净化控制器 内冷却并控制温度达到要求的温度、 置换出再生剂携带的气体介质后， 分两个输送管进 入反应器， 两个输送管设置催化剂流量控制闽门： 在第一输送管中来自再生剂净化控制 器的催化剂靠重力向下进入反应原料进入点下方， 与经再生立管来的再生剂混合， 降低 反应器内再生剂的温度，调节来自再生剂净化控制器的催化剂量控制再生剂和原料油接 触前的温度， 提高剂油比； 在第二输送管中净化后催化剂靠重力向下进入反应原料进料 点上方的气相反应区； 在反应器原料进料点以下设置催化剂测温点， 该温度控制再生剂 净化控制器第一输送管的闽门开度， 调节进入反应器的催化剂量； 用第二输送管上的闽 门开度控制进入反应器气相反应区的催化剂量。 本发明中， 再生剂净化取热冷却包括再生剂净化控制部分、 携带气体汽提、 催化剂 温度控制、 蒸汽调节和汽提气排出管线、 再生催化剂进出管线部分； 再生催化剂经一个 入口管进入， 经一个或两个输送管排出并送入反应器， 蒸汽在底部区域进入， 汽提介质 和再生剂携带气体在上部排出， 蒸汽进入管线上设置调节闽， 该调节闽由再生剂净化控 制器的催化剂温度控制或者由反应区相应位置的温度与再生剂净化控制器的催化剂温 度差控制。
本发明中，根据反应器进料点上方的气相反应区温度对再生剂净化控制器内催化剂 温度进行控制，使进入气相反应区的催化剂与气相反应区反应条件相适应；为实现要求， 分别在反应器气相反应区催化剂进入点和反应原料进入点之间的反应区及再生剂净化 控制器设置测温点， 由该两处温度差作为指标， 控制再生剂净化控制器操作介质管线调 节闽开度， 或者由反应器出口和再生剂净化控制器的温度差作为指标， 控制再生剂净化 控制器操作介质管线调节阀开度； 该调节阀进一步控制进入再生剂净化控制器的操作介 质量， 实现对再生剂净化控制器内催化剂和反应器反应温度的关联控制， 使进入反应器 气相反应区的催化剂始终适应反应器内的条件； 或者用再生剂净化控制器的温度作为指 标控制进入该再生剂净化控制器操作介质管线调节闽开度， 调节进入的流化介质量， 实 现对再生剂净化控制器弓 I出的温度的控制。
本发明的再生剂净化控制器用蒸汽作为操作介质，用蒸汽实现对再生剂携带烟气的 置换和对催化剂温度的控制； 或者设置空气和蒸汽两种操作介质， 蒸汽在空气下方进入 再生剂净化控制器； 调节空气量可以改变催化剂温度； 调节蒸汽量可以控制催化剂温度 和携带气体的置换效果。
本发明的再生剂净化控制器的催化剂从第二输送管在反应原料进入点起上方 0. 1秒 至 1.0秒的反应时间的空间内进入反应器气相反应区； 或者在反应原料进入点以上 1.0 米至 10米的区域内进入反应器气相反应区。
本发明再生剂净化控制器内上部设置换热管， 在冷却再生剂的同时， 反应原料在该 换热管内加热， 然后进入反应器； 或者在换热管内发生蒸汽； 再生剂净化控制器内下部 设置催化剂携带气体置换区。
本发明的反应原料在进入再生剂净化控制器换热管加热前加入占被加热原料重量 不大于 20%的水； 加热后再进入反应器。
本发明的反应再生剂控制方法的反应器气相反应区在冷却净化催化剂进入处设置 催化剂混合分配段， 该混合分配段直径大于该处反应器。 本发明的反应器气相反应区为提升管反应器， 或在冷却净化催化剂进入处混合分配 段上方设置扩径的反应段； 该扩径段内气相流速 1. 8m/s至 4.0m/s， 反应时间 3.0秒至 5.5秒。
图 1是本发明的一种反应区催化剂控制和再生剂净化取热冷却方法的工艺流程示意 图。再生催化剂分三路进入反应器 3，来自再生器 1的再生催化剂经再生立管 33直接进 入反应器 3底部的催化剂混合提升器 30， 完成反应后在汽提段 35汽提出携带的油气， 经待生立管 34返回再生器烧焦罐 12 (待生立管 34与再生器烧焦罐 12图 1中未标示， 请一并参考图 4所示） ， 其他来自再生器 1的催化剂经再生剂净化控制器 2处理后， 经 两个输送管 （再生剂净化控制器催化剂输送管 23、 24)在重力作用下送入反应器 3， 完 成反应后在汽提段 35汽提出携带的油气，经待生立管 34返回再生器烧焦罐 12:在第一 输送管（再生剂净化控制器催化剂输送管 24)中催化剂靠重力向下进入反应原料进入点 下方的催化剂混合提升器 30， 与经再生立管 33来的再生剂混合； 根据反应器原料进料 点以下反应温度（催化剂混合预提升段温度测温点 83 ) ， 调节第一输送管（再生剂净化 控制器催化剂输送管 24) 的滑闽 （再生剂净化控制器催化剂输送管滑闽 26) 开度， 控 制来自再生剂净化控制器 2的催化剂进入量； 在第二输送管（再生剂净化控制器催化剂 输送管 23 )中催化剂靠重力向下进入原料油进料点上方的反应器气相反应区 II，根据该 反应区催化剂进入点和反应原料进入点之间的测温点（原气相反应区补剂测温点 84)与 再生剂净化控制器 2第二输送管 (再生剂净化控制器催化剂输送管 23 )催化剂测温点（再 生剂净化控制器催化剂温度测温点 80)两点之间的温度差（净化控制器与气相反应区补 剂测温点的温度之差 81 ) ， 调节再生剂净化控制器 2操作介质 （蒸汽或空气 43、 蒸汽 44)管线调节闽（进再生剂净化控制器蒸汽或空气的调节闽 90、进再生剂净化控制器蒸 汽的调节闽 91 )开度， 控制再生剂净化控制器 2的温度（再生剂净化控制器催化剂温度 测温点 80) ， 向反应器气相反应区 II提供符合要求的催化剂； 蒸汽 44在再生剂净化控 制器 2底部进入再生剂净化控制器 2，向上经过再生剂净化控制器汽提区 27和再生剂净 化控制器冷却区 28， 在再生剂净化控制器顶部排气管线 29排出。
图 2是本发明的另一种反应区催化剂控制和再生剂净化取热冷却方法的工艺流程示 意图。再生催化剂分三路进入反应器 3，来自再生器 1的再生催化剂经再生立管 33直接 进入反应器 3底部的催化剂混合提升器 30，完成反应后在汽提段 35汽提出携带的油气， 经待生立管 34返回再生器烧焦罐 12 (待生立管 34与再生器烧焦罐 12图 1中未标示， 请一并参考图 4所示） ， 其他来自再生器 1的催化剂经再生剂净化控制器 2处理后， 经 两个输送管 （再生剂净化控制器催化剂输送管 23、 24)在重力作用下送入反应器 3， 完 成反应后经汽提段 35返回再生器烧焦罐 12: 在第一输送管 （再生剂净化控制器催化剂 输送管 24) 中催化剂靠重力向下进入反应原料进入点下方的催化剂混合提升器 30， 与 经再生立管 33来的再生剂混合； 根据反应器原料进料点以下反应温度 （催化剂混合预 提升段温度测温点 83 ) ， 调节第一输送管 （再生剂净化控制器催化剂输送管 24) 的滑 闽（再生剂净化控制器催化剂输送管滑闽 26)开度， 控制来自再生剂净化控制器 2的催 化剂进入量； 在第二输送管（再生剂净化控制器催化剂输送管 23 )中催化剂靠重力向下 进入原料油进料点上方的反应器气相反应区 II， 根据反应器 3 出口反应温度测温点 85 与再生剂净化控制器 2第二催化剂输送管（再生剂净化控制器催化剂输送管 23 )催化剂 测温点（再生剂净化控制器催化剂温度测温点 80)两点之间的温度差， 调节再生剂净化 控制器 2操作介质 （蒸汽或空气 43、 蒸汽 44) 管线的调节闽 （进再生剂净化控制器蒸 汽或空气的调节闽 90、 进再生剂净化控制器蒸汽的调节闽 91 ) 开度， 控制再生剂净化 控制器 2温度 （再生剂净化控制器催化剂温度测温点 80) ， 向反应器气相反应区 II提 供符合要求的催化剂；蒸汽 44在再生剂净化控制器 2底部进入再生剂净化控制器 2， 向 上经过再生剂净化控制器汽提区 27和再生剂净化控制器冷却区 28， 在再生剂净化控制 器顶部排气管线 29排出。
图 3是本发明的另一种反应区催化剂控制和再生剂净化取热冷却方法的工艺流程示 意图。 在蒸汽 44进入口上方向再生剂取热控制器 2送入压缩空气 40; 反应原料 （原料 油与会炼油的混合油 59) 在再生剂净化控制器 2换热管内加热后， 再经进料喷嘴 31进 入反应器 3 ; 其他与实施例 2相同。
图 4是本发明的一种反应区催化剂控制和再生剂净化取热冷却方法的装置示意图。 再生器 1与外取热器 13相连接外， 还与再生剂净化控制器 2相连接， 再生剂净化控制 器 2经两个输送管（再生剂净化控制器催化剂输送管 23、 24)与反应器 3相连接， 再生 剂净化控制器 2底部引出第一输送管（再生剂净化控制器催化剂输送管 24)到催化剂混 合提升器 30，再生剂净化控制器 2中下部引出第二输送管（再生剂净化控制器催化剂输 送管 23 )到催化剂分配器 32连接口位于反应器进料喷嘴 31的上方。而图 6中提升管反 应器气相反应区 Π上方设置扩径反应段 III (扩径反应区） 。 实施例：
实施例 1 :
本实施例中所用的反应区催化剂控制和再生剂取热冷却方法的装置参见图 5所示。 工艺流程参见图 7所示。
某年产 100 X 104t/a的石油烃催化裂化装置， 采用烧焦罐再生， 反应再生并列布置， 提升管反应器 3， 再生剂净化控制器 2产生中压蒸汽， 再生剂净化控制器 2采用自带汽 液分离器型式，气液分离器直接连接在再生剂净化控制器 2上，直径与净化控制器相同。 反应物料和实施例 1与原有技术的对比例反应条件见下表。
实施例 对比例
项目 单位 觀 单位 觀 原料油 52量 t/h 125 t/h 125 密度 Kg/m3 0.93 Kg/m3 0.93 残炭 W% 4.1 W% 4.1 原料油 52进料温度 °C 230 °C 230 反应出口温度 85 °c 500 °c 500 催化剂混合预提升器 30催化剂温度 °c 655 °c 690 气相反应区 Π补剂测温点温度 84 °c 530 °c 530 净化控制器 2第二引出口处与气相反应区 °c -10
II补剂测温点的温度之差 81
进料点到气相反应区 Π补剂点反应时间 s 0.2
总反应时间 s 2.6 s 2.6 再生剂量 t/h 834 t/h 834 来自第一催化剂输送管 24的催化剂量 t/h 157 t/h 0 进入气相反应区 Π的催化剂量 t/h 162 t/h 0 总反应剂油比 9.22 6.67 再生剂净化控制器用蒸汽量 g/h 980 Kg/h 0 本发明实施例 1与原油技术对比例的反再装置尺寸见下表。
实施例 对比例
项目 单位 觀 单位 觀 烧焦罐 12直径 Mm 5600 Mm 5800 烧焦罐 12高度 Mm 16000 Mm 16000 再生器 1稀相直径 Mm 9500 Mm 9800 反应器催化剂混合预提升器 30直径 Mm 1800 Mm 1600 反应器气相反应区 Π直径 Mm 1150 Mm 1000 反应器气相反应区 Π催化剂分配器 32直径 Mm 1800
再生剂净化控制器 2直径 Mm 2000
再生剂净化控制器 2内换热管面积 m2 90
再生剂净化控制器 2再生剂入口管直径 Mm 1100
第一催化剂输送管 24直径 Mm 350
第二催化剂输送管 23直径 Mm 350
再生剂净化控制器气体排出管 29直径 Mm 250
再生剂净化控制器 2蒸汽进入管直径 Mm 200 实施例 1与原油技术对比例反应产品分布见下表。
Figure imgf000014_0001
实施例 2:
本实施例中所用的反应区催化剂控制和再生剂取热冷却方法的装置参见图 6所示。 工艺流程参见图 8所示。
某年产 100 X 104t/a的石油烃催化裂化装置， 采用烧焦罐再生， 反应再生并列布置， 提升管反应器 3， 气相反应区 II上方设置扩径反应区 III， 其他条件与实施例 1相同。 反 应物料和实施例 2与原有技术的对比例反应条件见下表。 实施例 对比例
项目 单位 觀 单位 觀 原料油 52量 t/h 125 t/h 125 密度 Kg/m" 0.93 Kg/m" 0.93 残炭 W% 4.1 W% 4.1 原料油 52进料温度 °C 230 °C 230 反应出口温度 85 °c 500 °c 500 催化剂混合预提升器温度 83 °c 655 °c 690 气相反应区 Π补剂测温点温度 84 °c 530 °c 530 净化控制器 2第二引出口处与气相反应区 °c -10
II补剂测温点的温度之差 81
进料点到气相反应区 Π补剂点反应时间 s 0.2
总反应时间 s 5.4 s 5.4 反应器扩径段 m反应时间 s 4.0 s 4.0 再生剂量 t/h 834 t/h 834 从第一输送管 24进入的冷却催化剂量 t/h 157 t/h 0 进入气相反应区 Π催化剂量 t/h 162 t/h 0 总反应剂油比 9.22 6.67 再生剂净化控制器 2用蒸汽量 g/h 980 Kg/h 0 本发明实施例 2与原油技术对比例的反再装置尺寸见下表。
实施例 对比例
项目 单位 觀 单位 觀 烧焦罐 12直径 Mm 5600 Mm 5800 烧焦罐 12高度 Mm 16000 Mm 16000 再生器 1稀相直径 Mm 9500 Mm 9800 反应器催化剂混合预提升器 30直径 Mm 1800 Mm 1600 反应器气相反应区 Π直径 Mm 1150 Mm 1000 反应器气相反应区 Π催化剂分配器 32直径 Mm 1800
反应器反应扩径段 III直径 Mm 2700 Mm 2200 再生剂净化控制器 2直径 Mm 2000 再生剂净化控制器 2内换热管面积 m1 90
再生剂净化控制器 2再生剂入口管直径 Mm 1100
第一催化剂输送管 24直径 Mm 350
第二催化剂输送管 23直径 Mm 350
再生剂净化控制器气体排出管 29直径 Mm 250
再生剂净化控制器 2蒸汽进入管直径 Mm 200 实施例 2与原油技术对比例反应产品分布见下表。
实施例 对比例 成分 单位 觀 单位 觀 干气 w% 2.8 w% 3.2 液化气 w% 12 w% 12.2 汽油 w% 42 w% 41.9 柴油 w% 30.1 w% 29.5 重油 w% 3.5 w% 3.3 焦炭 w% 9.1 w% 9.4 损失 w% 0.5 w% 0.5 合计 w% 100 w% 100

Claims

权利要求书
1. 一种反应区催化剂控制和再生剂净化取热冷却方法， 用于石油烃类原料或醇类 原料催化反应过程； 其特征在于， 该方法包括对反应的控制和对进入反应器的催化剂的 控制， 方法中所用装置包括有以下部分： 反应器， 催化剂再生器， 再生剂净化控制器， 催化剂输送管道； 对反应的控制包括液相接触气化反应控制， 气相反应过程控制， 反应 器出口温度控制； 对进入反应器的催化剂的控制包括再生剂温度控制和进入反应器的催 化剂携带气体的净化控制； 再生剂进入净化控制器后被换热管冷却控制温度， 同时用蒸 汽置换出携带的气体， 包括氮气、 二氧化碳和氧气， 达到要求的温度和气体携带要求后 的催化剂从催化剂输送管靠重力向下进入反应器反应原料进入点下方或 /和反应原料和 催化剂接触气化区上方， 使反应器实现对反应前、 液相气化反应后和反应出口反应条件 的多级控制， 同时限制再生剂携带的氮气、 氧气和二氧化碳进入反应器。
2. 根据权利要求 1所述的方法， 其特征在于， 对反应器的催化剂的控制方法中， 再生催化剂分三路进入反应器， 一路来自再生器的再生催化剂经再生立管直接进入反应 器底部， 其他再生剂在净化控制器内冷却并控制温度达到要求的温度、 置换出再生剂携 带的气体介质后， 分两个输送管进入反应器， 两个输送管设置催化剂流量控制闽门： 在 第一输送管中来自再生剂净化控制器的催化剂靠重力向下进入反应原料进入点下方， 与 经再生立管来的再生剂混合， 降低反应器内再生剂的温度， 调节来自再生剂净化控制器 的催化剂量控制再生剂和原料油接触前的温度， 提高剂油比； 在第二输送管中净化后催 化剂靠重力向下进入反应原料进料点上方的气相反应区； 在反应器原料进料点以下设置 催化剂测温点， 该温度控制再生剂净化控制器第一输送管的闽门开度， 调节进入反应器 的催化剂量； 用第二输送管上的闽门开度控制进入反应器气相反应区的催化剂量。
3. 根据权利要求 1或 2所述的方法， 其特征在于， 再生剂净化取热冷却包括再生 剂净化控制部分、 携带气体汽提、 催化剂温度控制、 蒸汽调节和汽提气排出管线、 再生 催化剂进出管线部分； 再生催化剂经一个入口管进入， 经一个或两个输送管排出并送入 反应器， 蒸汽在底部区域进入， 汽提介质和再生剂携带气体在上部排出， 蒸汽进入管线 上设置调节闽， 该调节闽由再生剂净化控制器的催化剂温度控制或者由反应区相应位置 的温度与再生剂净化控制器的催化剂温度差控制。
4. 根据权利要求 1或 3所述的方法， 其特征在于， 根据反应器进料点上方的气相 反应区温度对再生剂净化控制器内催化剂温度进行控制，使进入气相反应区的催化剂与 气相反应区反应条件相适应； 分别在反应器气相反应区催化剂进入点和反应原料进入点 之间的反应区及再生剂净化控制器设置测温点， 由该两处温度差作为指标， 控制再生剂 净化控制器操作介质管线调节闽开度， 或者由反应器出口和再生剂净化控制器的温度差 作为指标， 控制再生剂净化控制器操作介质管线调节闽开度； 该调节闽进一步控制进入 再生剂净化控制器的操作介质量， 实现对再生剂净化控制器内催化剂和反应器反应温度 的关联控制， 使进入反应器气相反应区的催化剂始终适应反应器内的条件； 或者用再生 剂净化控制器的温度作为指标控制进入该再生剂净化控制器操作介质管线调节闽开度， 调节进入的流化介质量， 实现对再生剂净化控制器引出的温度的控制。
5. 根据权利要求 1或 3所述的方法， 其特征在于， 再生剂净化控制器用蒸汽作为 操作介质， 用蒸汽实现对再生剂携带烟气的置换和对催化剂温度的控制； 或者设置空气 和蒸汽两种操作介质， 蒸汽在空气下方进入再生剂净化控制器； 调节空气量改变催化剂 温度； 调节蒸汽量控制催化剂温度和携带气体的置换效果。
6. 根据权利要求 1或 3所述的方法， 其特征在于， 再生剂净化控制器的催化剂从 第二输送管在反应原料进入点起上方 0. 1秒至 1.0秒的反应时间的空间内进入反应器气 相反应区； 或者在反应原料进入点以上 1.0米至 10米的区域内进入反应器气相反应区。
7. 根据权利要求 1或 3所述的方法， 其特征在于， 再生剂净化控制器内上部设置 换热管， 在冷却再生剂的同时， 反应原料在该换热管内加热， 然后进入反应器； 或者在 换热管内发生蒸汽； 再生剂净化控制器内下部设置催化剂携带气体置换区。
8. 根据权利要求 1或 7所述的方法， 其特征在于， 反应原料在进入再生剂净化控 制器换热管加热前加入占被加热原料重量不大于 20%的水； 加热后再进入反应器。
9. 根据权利要求 1所述的方法， 其特征在于， 反应器气相反应区在冷却净化催化 剂进入处设置催化剂混合分配段， 该混合分配段直径大于该处反应器。
10. 根据权利要求 1所述的方法，其特征在于，反应器气相反应区为提升管反应器， 或在冷却净化催化剂进入处混合分配段上方设置扩径的反应段； 该扩径段内气相流速 1. 8m/s至 4.0m/s， 反应时间 3.0秒至 5.5秒。
11. 一种用于实现权利要求 1〜10任一项所述方法的反应区催化剂控制和再生剂净 化取热冷却装置， 该装置包括再生器、 外取热器、 再生剂净化控制器、 反应器， 其中： 再生器与外取热器相连接， 还与再生剂净化控制器相连接， 再生剂净化控制器经两 个输送管与反应器相连接， 再生剂净化控制器底部引出第一输送管到催化剂混合提升 器， 再生剂净化控制器中下部引出第二输送管到位于反应器进料喷嘴的上方的催化剂分 配器连接口。
12、 根据权利要求 11所述的装置， 其中， 反应器为提升管反应器， 提升管反应器 气相反应区上方设置扩径反应区。
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