CN115007074B - Catalyst continuous circulation reaction experimental device with double reactors - Google Patents
Catalyst continuous circulation reaction experimental device with double reactors Download PDFInfo
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- CN115007074B CN115007074B CN202110473509.8A CN202110473509A CN115007074B CN 115007074 B CN115007074 B CN 115007074B CN 202110473509 A CN202110473509 A CN 202110473509A CN 115007074 B CN115007074 B CN 115007074B
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- 239000003054 catalyst Substances 0.000 title claims abstract description 296
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 50
- 238000010438 heat treatment Methods 0.000 claims abstract description 98
- 238000011069 regeneration method Methods 0.000 claims abstract description 35
- 238000009413 insulation Methods 0.000 claims abstract description 33
- 230000008929 regeneration Effects 0.000 claims abstract description 24
- 238000004321 preservation Methods 0.000 claims abstract description 14
- 238000000034 method Methods 0.000 claims abstract description 11
- 239000002826 coolant Substances 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 16
- 238000004062 sedimentation Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 230000000295 complement effect Effects 0.000 claims 1
- 238000002474 experimental method Methods 0.000 abstract description 5
- 238000005259 measurement Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 11
- 238000004523 catalytic cracking Methods 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 239000011324 bead Substances 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 230000017525 heat dissipation Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
-
- 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
-
- 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
- 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
- C10G11/187—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00389—Controlling the temperature using electric heating or cooling elements
- B01J2208/00407—Controlling the temperature using electric heating or cooling elements outside the reactor bed
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention discloses a catalyst continuous circulation reaction experimental device with double reactors, which is provided with a reactor A, a reactor B, a stripper and a regenerator, wherein the parts are communicated through pipelines to realize continuous circulation of a catalyst between the reactor and the regenerator; the outside of each part of the device is respectively provided with a heat preservation layer, a heating furnace or a heat insulation and heat compensation heating furnace, so that the temperature control of each part in the reaction regeneration process is realized, and the catalyst circulation metering unit is arranged, so that the measurement of the catalyst circulation in the experimental process is realized. The invention provides a process experiment device capable of carrying out real catalyst grading circulation, which can carry out various circulation scheme experiments of various forms of various reactors and regenerated catalysts.
Description
Technical Field
The invention relates to a catalyst continuous circulation gas-solid catalytic reaction experimental device in the petrochemical field, in particular to a double-reactor catalyst continuous circulation reaction experimental device.
Background
Catalytic cracking is an important means for lightening heavy oils. Catalytic cracking processes are an important factor affecting the product distribution of catalytic cracker units. The prior small-sized riser devices in the laboratory are basically of conventional riser types, and have the main functions of evaluating the performance of a catalytic cracking catalyst and evaluating raw oil, and basically have no process experiment capability. The existing laboratory riser device does not have the function of measuring the circulating amount of the catalyst, can only calculate according to the reaction heat balance, and has large error. The industrial catalytic cracking device is an adiabatic reaction, and the heating furnace directly heats the riser reactor in the existing laboratory riser device, so that the adiabatic reaction cannot be carried out, and the calculation error of the catalyst circulation amount is larger; because the feeding amount of the experimental device is small, the heat dissipation capacity of the device is large, and the real reaction heat process is difficult to realize only through heat preservation, so that experimental data deviation is caused.
Disclosure of Invention
The invention aims to overcome the defects of the conventional riser experimental device and provides a double-reactor catalyst continuous circulation reaction experimental device.
The invention provides a catalyst continuous circulation reaction experimental device of double reactors,
Is provided with a reactor A, a reactor B, a stripper, a regenerator A and one or more regenerated catalyst supply pipes; the top of the stripper is provided with a stripping sedimentation device, and the bottom of the stripper is provided with a spent catalyst supply pipe A; the top of the regenerator A is provided with a regeneration settler A, and the bottom of the regenerator A is provided with a regenerated catalyst supply pipe A; the regenerated catalyst supply pipe A is communicated with the lower part of the reactor A, the outlet of the reactor A is communicated with the stripper or the stripping settler, and the outlet of the reactor B is communicated with the stripper or the stripping settler;
The device is provided with a spent catalyst conveying pipe A (or conveying pipe A), the inlet of the spent catalyst conveying pipe A is communicated with a spent catalyst supply pipe A, the outlet of the spent catalyst conveying pipe A is communicated with a regenerator A or a regeneration settler A, and the spent catalyst stripped by the stripper is conveyed to the regenerator A through the spent catalyst conveying pipe A; the lower part of the reactor B is communicated with the bottom of the regenerator A through a regenerated catalyst supply pipe B, and the regenerated catalyst supply pipes are communicated with each other to realize continuous circulation of the catalyst among the reactor, the reactor B and the regenerator A respectively; a catalyst circulation metering unit A is arranged on a spent catalyst conveying pipe A;
A heating furnace, a heat insulation and heat compensation heating furnace or a heat preservation layer is arranged outside (the outer wall or the outer side) the reactor A, the reactor B, the stripper, the catalyst supply pipe A to be regenerated, the regenerator A and the regenerated catalyst supply pipes. Regenerated catalyst as used herein refers to catalyst from an experimental set-up called a "regenerator" whose carbon content and/or temperature of the catalyst exiting the regenerator may vary. The invention controls the carbon content of the catalyst entering the reactor or the catalyst flowing out of the regenerator A by controlling the regeneration temperature in the regenerator A and the air quantity entering the regenerator A or the oxygen content of the gas entering the regenerator A; the temperature of the catalyst entering the reactor is controlled by controlling the temperature of the catalyst in the regenerated catalyst feed pipe. In practice, the present invention provides for the installation of feed nozzles at the inlet of each reactor; the feeding nozzle is provided with a reactant feeding pipe and an atomization steam feeding pipe, the top of the stripping settler is provided with an oil gas outlet, and reaction products and stripping medium flow out from the outlet; the bottom of the regenerator is provided with a burnt gas inlet pipe, and the top of the regenerator is provided with a flue gas outlet. In a specific embodiment, reactor a and reactor B take the form of risers.
In the catalyst continuous circulation reaction experimental device of the double reactors, preferably, the heating furnace is provided with a heating furnace wire and an external heat preservation layer;
the heat insulation and supplementary heating furnace is provided with an inner heat insulation layer, a heating furnace wire and an outer heat preservation layer;
The temperature controller comprises a temperature thermocouple (or called temperature measuring thermocouple) and a heating furnace wire power controller; the power controller is arranged on the heating furnace wire circuit, the temperature thermocouple signal is fed back to the power controller, and the power controller adjusts the power of the heating furnace wire to realize temperature control. In the specific implementation of the invention, valves, or plug valves or slide valves are arranged on the regenerated catalyst supply pipe and the spent catalyst supply pipe to control the circulation quantity of the catalyst; the reaction temperature signal of the temperature thermocouple of the reactor enters the controller, and the controller controls the valve on the regenerated catalyst supply pipe to adjust the circulating quantity of the catalyst so as to realize the control of the reaction temperature.
In the above-mentioned double-reactor catalyst continuous circulation reaction experimental device, preferably, heating furnaces are arranged outside the regenerator a and each regenerated catalyst supply pipe or are arranged in sections, so as to supply heat to the catalyst in the regenerator a and the regenerated catalyst supply pipes respectively; temperature thermocouples are respectively arranged or sectionally arranged on the inner side and the outer side of the regenerator A and the regenerated catalyst supply pipe. When the method is implemented, the heat provided by the reaction raw coke oxidation regeneration can not meet the heat requirement of the reaction due to the small feeding amount of the experimental device and the large heat dissipation and heat loss, and the heat compensation of the regenerator is realized by a method of externally compensating the heat of the regenerator, so that the control of the regeneration temperature is realized. In the specific implementation, a heating furnace is arranged outside the regenerator A in a sectional manner, and after power is supplied, the heating furnace is converted into heat to supply heat to the catalyst in the regenerator A; meanwhile, a power controller is arranged on a heating furnace wire power supply line, the power supply is adjusted to realize the heat supply quantity of the heating furnace wire, and the temperature in the regenerator A is controlled; a high temperature zone formed outside the regenerator A by the heating furnace wire and a temperature thermocouple are arranged in the regenerator A; and the power supply power of the heating furnace wires outside the regenerator A is regulated according to the temperature of a high-temperature area formed by the heating furnace wires outside the regenerator A or according to the set power. Similarly, in the concrete implementation, a heating furnace is arranged outside the regenerated catalyst supply pipe or a heating furnace is arranged in sections, and the heating furnace wire is powered to realize the temperature rise outside the catalyst supply pipe and control the temperature of the catalyst in the regenerated catalyst supply pipe; and temperature thermocouples are arranged in and outside the regenerated catalyst supply pipe, and the power supply of the heating furnace wires outside the regenerated catalyst supply pipe is regulated according to the temperature of a high temperature area formed by the heating furnace wires outside the regenerated catalyst supply pipe or according to the set power. In the invention, a heating furnace can be arranged outside the stripper in a sectionalized way, and after power is supplied, the heating furnace is converted into heat to supply heat to the catalyst in the stripper; the heating furnace wire power supply line is provided with a power controller, the power supply is regulated to realize the heat supply of the heating furnace wire, and the temperature in the stripper is controlled; a high temperature area formed outside the stripper and a temperature thermocouple are arranged in the stripper; and the power supply power of the heating furnace wires outside the stripper is regulated according to the temperature of a high-temperature area formed by the heating furnace wires outside the stripper or according to the set power.
In the above-mentioned double-reactor catalyst continuous circulation reaction experimental device, preferably, the reactor A and/or the reactor B are designed into a sectional detachable structure, and each reaction section realizes sectional detachment and replacement of the reactor through flanges or threads; the diameters of the reaction sections are the same or different.
In the above-mentioned continuous circulation reaction experimental device for the double-reactor catalyst, preferably, heat insulation and heat compensation heating furnaces are arranged or sectionally arranged outside the outer walls of the reactor A and the reactor B, and meanwhile, temperature thermocouples are arranged or sectionally arranged in the corresponding reactor and the heating furnace wire area outside the reactor. In the invention, a heat insulation and heat compensation heating furnace is arranged outside the reactor wall, and after the heating furnace wire is powered, the heating furnace wire is converted into heat to improve the temperature outside the reactor, so that the temperature difference between the outside and inside the reactor is controlled; the external temperature of the reactor is the same as or close to the internal temperature of the reactor through the external heat supplement of the reactor, so that the heat dissipation of the reactor outwards or the heat transfer inwards is limited, the heat balance of the actual reaction and the heat supply of the catalyst is realized or the heat insulation of the external wall of the reactor is realized; in the specific implementation, a power controller is arranged on a heating furnace wire power supply circuit, the power supply is regulated to realize the heat supply quantity of the heating furnace wire, and the temperature outside the reactor is controlled; temperature thermocouples are arranged in the reactor and in the heating furnace wire area outside the reactor.
In the above-mentioned double-reactor catalyst continuous circulation reaction experimental device, preferably, a regenerator B and a spent catalyst conveying pipe B (or conveying pipe B) are provided, the regenerator B is provided with a regeneration settler B, and the bottom of the stripper is provided with a spent catalyst supply pipe B;
The lower part of the reactor B is communicated with the bottom of the regenerator B through a regenerated catalyst supply pipe B311; the inlet of the spent catalyst conveying pipe B is communicated with the spent catalyst supply pipe B, the outlet of the spent catalyst conveying pipe B is communicated with the regenerator B or the regeneration settler B, the continuous circulation of the catalyst among the reactor A and the reactor B, the regenerator A and the regenerator B is realized through mutual communication, the regenerated catalyst supply pipe A supplies the catalyst to the reactor A, the regenerated catalyst supply pipe B supplies the catalyst to the reactor B, and the spent catalyst conveying pipe B is provided with a catalyst circulation metering unit B;
and an insulating layer or a heating furnace is arranged outside the regenerator B and the spent catalyst supply pipe B. In specific implementation, the device is provided with two regenerators which are respectively communicated with two regenerated catalyst supply pipes and supply catalysts to the two reactors; the experimental device is characterized in that a spent catalyst conveying pipe is arranged between a stripper and two regenerators, the stripper is provided with two spent catalyst supply pipes which are respectively communicated with the two spent catalyst conveying pipes, so that spent catalyst is conveyed to the two regenerators, further, catalyst circulation among the two regenerators, the two reactors and the stripper is realized, and catalyst circulation metering units are respectively arranged on the two spent catalyst conveying pipes for controlling catalyst circulation.
In the above-mentioned double-reactor catalyst continuous circulation reaction experimental device, preferably, the catalyst circulation metering unit a or the catalyst circulation metering unit B includes a cooling pipe correspondingly disposed outside the spent catalyst conveying pipe a or the spent catalyst conveying pipe B, the cooling pipe and the spent catalyst conveying pipe a or the spent catalyst conveying pipe B form an inner and outer sleeve or ring pipe structure, and an annular space between the cooling pipe and the spent catalyst conveying pipe a or the spent catalyst conveying pipe B forms a cooling medium channel; a cooling medium inlet pipe and a cooling medium outlet pipe are respectively arranged at two ends of the cooling pipe; an insulation layer is arranged outside the cooling pipe;
A lower inlet catalyst temperature thermocouple and an upper outlet catalyst temperature thermocouple are arranged on the spent catalyst conveying pipe A or the spent catalyst conveying pipe B, and the inlet catalyst temperature thermocouple and the outlet catalyst temperature thermocouple are respectively positioned at the bottom end and the top end of the cooling pipe; a cooling medium outlet temperature thermocouple is arranged at the bottom end of the cooling pipe or on the cooling medium outlet pipe, and a cooling medium inlet temperature thermocouple is arranged at the top end of the cooling pipe or on the cooling medium inlet pipe.
In the above-mentioned double-reactor catalyst continuous circulation reaction experiment device, preferably, the reactor a and/or the reactor B are provided with one or more catalyst inlets, and the regenerator a and/or the regenerator B are provided with regenerated catalyst supply pipes corresponding to the catalyst inlets, so that the regenerator a and/or the regenerator B can supply catalyst to the reactor a and/or the reactor B through the regenerated catalyst supply pipes via the catalyst inlets. When the invention is implemented, the reactor can be connected in series in two different fluidization modes according to the position up and down, and the upper part is provided with a diameter expansion section. In the experimental device of the present invention, one or more catalyst outlets may be provided in the regenerator and respectively connected to the regenerated catalyst supply pipes to supply the catalyst to the two reactors, and in a specific implementation process, 1 to 4 regenerated catalyst supply pipes are preferably provided, and these regenerated catalyst supply pipes may be simultaneously connected to one regenerator, or one of them is connected to the regenerator a, and the other is connected to the regenerator B, so as to form one or more loops of the catalyst between the reactors and the regenerator.
In the above-described double-reactor catalyst continuous circulation reaction experimental apparatus, preferably, the regeneration temperature and the amount of intake air or the amount of oxygen in the gas of the regenerator a or the regenerator B are controlled to control the carbon content of the catalyst entering the reactor a and/or the reactor B, and the temperature of the catalyst in the regenerated catalyst supply pipe a and the regenerated catalyst supply pipe B is controlled to control the temperature of the catalyst entering the reactor a and/or the reactor B.
Effects of the invention
The two reactors of the invention can realize the respective reactions of different raw materials; the invention has a catalyst circulation metering unit, can more accurately measure the circulation of the catalyst, and increases the reliability of experiments and the guidance of industrial catalytic cracking operation; according to the invention, through the special design of the reaction zone heating furnace, the adiabatic reaction can be realized, so that the reaction result is more reliable. The temperature of the regenerated catalyst entering the reaction area is flexibly adjusted by controlling the power of the regenerated catalyst supply pipe heating furnace.
Drawings
Fig. 1: the experimental device provided with the single regenerator is structurally schematic;
fig. 2: the experimental device provided with two regenerators is structurally schematic;
Fig. 3: a schematic view of the structure of a heating furnace provided by the regenerator A in FIG. 1;
fig. 4: the specific structure of the heat insulation and heat compensation heating furnace arranged in the reactor A in FIG. 1 is schematically shown;
Fig. 5: the catalyst circulation amount measuring unit A in FIG. 1 is schematically shown in structure.
Description of the drawings:
101-feed nozzle, 102-pre-lift section, 103-reactor A, 104-riser A insulation and make-up furnace, 105-riser A outlet temperature thermocouple, 107-stripper expansion zone, 108-stripper temperature thermocouple, 109-stripping settler, 110-stripping settler filter, 111-oil gas outlet, 112-stripper, 113-stripper furnace, 114-stripping steam inlet, 115-spent catalyst feed pipe A, 116-spent catalyst feed pipe A plug valve or slide valve, 117-spent catalyst feed pipe B, 118-spent catalyst feed pipe B plug valve or slide valve, 201-transfer wind inlet A, 202-spent catalyst transfer pipe A, 203-catalyst circulation metering unit A, 205-regeneration settler A, 206-regeneration settler A gas outlet, 207-regeneration settler A filter, 208-regenerator A, 209-regenerator A furnace, 210-regenerator A air inlet, 211-regeneration catalyst supply pipe A, 212-regeneration catalyst supply pipe A furnace, 213-regeneration catalyst supply pipe A plug or slide valve, 214-regeneration catalyst supply pipe A return temperature thermocouple, 301-transfer wind inlet B, 302-spent catalyst transfer pipe B, 303-catalyst circulation metering unit B, 305-regeneration settler B, 306-regeneration settler B outlet, 307-regeneration settler B filter, 308-regenerator B, 309-regenerator B furnace, 310-regenerator B air inlet, 311-regeneration catalyst supply pipe B, 312-regenerated catalyst feed pipe B heating furnace, 313-regenerated catalyst feed pipe B plug valve or slide valve, 314-regenerated catalyst feed pipe B return temperature thermocouple, 401-feed nozzle, 402-pre-lift section, 403-reactor B, 404-riser B heat insulation and make-up heating furnace, 405-riser B outlet temperature thermocouple, 502-inlet catalyst temperature thermocouple, 503-outlet catalyst temperature thermocouple, 504-cooling medium inlet, 505-cooling medium outlet, 506-cooling medium inlet temperature thermocouple, 507-cooling medium outlet temperature thermocouple, 508-cooling pipe, 509-heat insulating layer, 601-equipment pipe wall, 602-heat insulating layer, 603-heating furnace wire or electric heating wire, 604-insulating bowl bead, 605-heat insulating layer, 606-furnace heat insulating housing, TC temperature control signal (temperature display), KW power control signal, TI temperature display.
Detailed Description
The invention is described in further detail below with reference to the drawings and the detailed description. The drawings and detailed description are not intended to limit the scope of the invention as claimed.
As shown in fig. 1, a double-reactor catalyst continuous circulation reaction experimental device is provided with a reactor a103, a reactor B403, a stripper 112 and a regenerator a208; a stripping settler 109 is arranged at the top of a stripper expanding region 107 at the upper part of a stripper 112, a spent catalyst supply pipe A115 is arranged at the bottom, the spent catalyst supply pipe A115 is provided with a spent catalyst supply pipe A plug valve or a slide valve 116, the stripping settler 109 is provided with a stripping settler filter 110 and an oil gas outlet 111, a stripping steam inlet 114 is arranged at the lower part of the stripper 112, and reaction products and stripping medium (such as steam) of the reactor flow out of the oil gas outlet 111 through the stripping settler filter 110; a regeneration settler A205 is arranged at the top of the regenerator A208, a regenerated catalyst supply pipe A211, a regenerated catalyst supply pipe B311 and a regenerator A air inlet 210 are arranged at the bottom, the regeneration settler A205 is provided with a regeneration settler A filter 207 and a regeneration settler A gas outlet 206, oxygen-containing air enters the regenerator A208 to burn and realize catalyst regeneration, regenerated flue gas flows out of the regeneration settler A gas outlet 206 through the regeneration settler A filter 207, a regenerated catalyst supply pipe A plug valve or a slide valve 213 is arranged on the regenerated catalyst supply pipe A211, and a regenerated catalyst supply pipe B plug valve or a slide valve 313 is arranged on the regenerated catalyst supply pipe B311; the regenerated catalyst supply pipe A211 is communicated with a pre-lifting section A102 at the bottom of the reactor A103, a feeding nozzle A101 is arranged at the inlet of the pre-lifting section A102, a reactor A outlet temperature thermocouple 105 is arranged at the outlet of the reactor A103, the regenerated catalyst supply pipe B311 is communicated with a pre-lifting section B402 at the bottom of the reactor B403, a feeding nozzle B401 is arranged at the inlet of the pre-lifting section B402, a reactor B outlet temperature thermocouple 405 is arranged at the outlet of the reactor B403, and the outlet of the reactor A103 and the outlet of the reactor B403 are both communicated with a stripper expanding region 107 of the stripper 112; the regenerator A208 is communicated with a spent catalyst supply pipe A115 through a spent catalyst conveying pipe A202, an air conveying inlet A201 is formed in the bottom of the spent catalyst conveying pipe A202, the outlet of the spent catalyst conveying pipe A202 is communicated with the upper part of the regenerator A208, spent catalyst stripped by the stripper 112 enters the spent catalyst conveying pipe A202, and conveying air introduced by the air conveying inlet A201 is conveyed to the regenerator A208, so that continuous circulation of the catalyst among the reactor A103, the reactor B403 and the regenerator A208 is realized through mutual communication;
In specific implementation, a catalyst circulation metering unit a203 is disposed on a spent catalyst conveying pipe a202, as shown in fig. 5, the catalyst circulation metering unit a203 includes a cooling pipe 508 disposed outside the spent catalyst conveying pipe a202, the cooling pipe 508 and the spent catalyst conveying pipe a202 form an inner and outer sleeve or loop structure, and an annular space between the cooling pipe 508 and the spent catalyst conveying pipe a202 forms a cooling medium channel; a cooling medium inlet 504 and a cooling medium outlet 505 are respectively arranged at two ends of the cooling pipe 508; a heat insulation layer 509 is arranged outside the cooling pipe 508; the method comprises the steps that a lower inlet catalyst temperature thermocouple 502 and an upper outlet catalyst temperature thermocouple 503 are arranged on a spent catalyst conveying pipe A202, and the inlet catalyst temperature thermocouple 502 and the outlet catalyst temperature thermocouple 503 are respectively positioned at the bottom end and the top end of a cooling pipe 508; a cooling medium outlet temperature thermocouple 507 is provided at the cooling medium outlet 505, and a cooling medium inlet temperature thermocouple 506 is provided at the cooling medium inlet 504; the specific structure of the catalyst circulation amount measuring unit is similar to the following embodiments, and will not be described again;
In the experimental apparatus of the present invention, heating furnaces, namely, a stripper heating furnace 113, a regenerator a heating furnace 209, a regenerated catalyst supply pipe a heating furnace 212, and a regenerated catalyst supply pipe B heating furnace 312 are provided outside the stripper 112, the regenerator a208, the regenerated catalyst supply pipe a211, and the regenerated catalyst supply pipe B311, respectively. The structure of the regenerator A heating furnace 209 is shown in fig. 3, the regenerator A heating furnace 209 is arranged on the outer side of the equipment pipe wall 601 of the regenerator A208, and consists of a heating furnace wire 603 and an external heat preservation layer 605, the heating furnace wire 603 is sheathed with an insulating bowl bead 604, the heat preservation layer 605 is arranged on the periphery of the heating furnace wire 603, and the heat preservation layer 605 is sheathed with a furnace heat insulation shell 606; the stripper heating furnace 113, the regenerated catalyst supply pipe a heating furnace 212 and the regenerated catalyst supply pipe B heating furnace 312 have the same structure as the regenerator a heating furnace 209, and the specific construction of the heating furnaces is similar to that of other embodiments, and will not be described again;
The heat insulation and heat compensation heating furnace 104 of the lifting pipe A is arranged outside the reactor A103, the heat insulation and heat compensation heating furnace 404 of the lifting pipe B is arranged outside the reactor B403, the structure of the heat insulation and heat compensation heating furnace 104 of the lifting pipe A is shown in figure 4, the heat insulation and heat compensation heating furnace 104 of the reactor A is arranged outside the pipe wall 601 of the reactor A103, the heat insulation and heat compensation heating furnace is composed of an inner heat insulation layer 602, a heating furnace wire 603 and an outer heat preservation layer 605, the heating furnace wire 603 is sheathed with an insulating bowl bead 604, the heat preservation layer 605 is arranged on the periphery of the heating furnace wire 603, and the heat preservation layer 605 is sheathed with a furnace heat insulation shell 606; the heat insulation and heat compensation heating furnace 404 of the reactor B4 has the same structure as the heat insulation and heat compensation heating furnace 104 of the lifting pipe A, and other embodiment modes are similar to those of the heat insulation and heat compensation heating furnace and are not repeated;
In specific implementation, as shown in fig. 1, the heating furnace or the heat insulation and compensation heating furnace is provided with a power controller on a heating furnace wire circuit, a high temperature region formed by heating furnace wires outside the wall of a regenerator a208 and a temperature thermocouple in the regenerator a208 are provided, a regenerated catalyst supply pipe a return temperature thermocouple 214 is provided inside and outside a regenerated catalyst supply pipe a211, a regenerated catalyst supply pipe B return temperature thermocouple 314 is provided inside and outside a regenerated catalyst supply pipe B311, a temperature thermocouple is provided in a high temperature region formed by heating furnace wires outside the wall of a reactor a103 and a reactor a103, a temperature thermocouple is provided in a high temperature region formed by heating furnace wires outside the wall of a reactor B403 and a temperature thermocouple is provided in a stripper 113, and a temperature thermocouple 105, a temperature thermocouple 405 at the outlet of a reactor B and a temperature thermocouple of a catalyst circulation metering unit a203 are respectively connected with the power controller, so as to form a temperature control system for the device; when the device works, temperature signals of the temperature thermocouples are fed back or transmitted to a power controller, and the power controller adjusts the heating power of the heating furnace wires to realize temperature control of the catalyst entering the reaction regeneration part of the device, such as temperature control of the catalyst entering the regenerator A208, the regenerated catalyst supply pipe A211, the regenerated catalyst supply pipe B311 and the catalyst in the catalyst circulation metering unit.
The catalyst continuous circulation reaction experimental device of the double reactor shown in fig. 2 is further provided with a regenerator B308 and a spent catalyst conveying pipe B302, wherein the regenerator B308 is provided with a regeneration settler B305, the bottom of the stripper 112 is provided with two spent catalyst supply pipes, namely a spent catalyst supply pipe A115 and a spent catalyst supply pipe B117, and a pre-lifting section B402 at the lower part of the reactor B403 is communicated with the bottom of the regenerator B308 through a regenerated catalyst supply pipe B311; the inlet of a spent catalyst conveying pipe B302 is communicated with a spent catalyst supply pipe B117, the outlet is communicated with a regenerator B308, other parts of the device are in the same structure as in FIG. 1, the parts of the device are communicated with each other to realize continuous circulation of catalyst among a reactor A103, a reactor B403, a regenerator A208 and the regenerator B308, a regenerated catalyst supply pipe A211 supplies catalyst to the reactor A103, a regenerated catalyst supply pipe B311 supplies catalyst to the reactor B403, and a catalyst circulation metering unit B303 is arranged on the spent catalyst conveying pipe B302; a regenerator a furnace 309 is provided outside the regenerator B308. When the experimental device specifically works, two spent catalyst supply pipes are arranged at the bottom of the stripper 112, a part of spent catalyst enters the bottom of a spent catalyst conveying pipe A202 through a spent catalyst supply pipe A115 and passes through a spent catalyst supply pipe A plug valve or a slide valve 116 to be conveyed to a regenerator A208, and regenerated catalyst enters a pre-lifting section A102 of a reactor A103 through a regenerated catalyst supply pipe A211 and passes through a regenerated catalyst supply pipe A plug valve or a slide valve A213 to be contacted with raw oil entering from a nozzle A101 to be conveyed upwards for reaction; the other part of spent catalyst enters the bottom of a spent catalyst conveying pipe B302 through a spent catalyst supply pipe B117 and a spent catalyst supply pipe B plug valve or a slide valve 118 and is conveyed to a regenerator B308, the regenerated catalyst enters a pre-lifting section B402 of a reactor B403 through a regenerated catalyst supply pipe B311 and a regenerated catalyst supply pipe B plug valve or a slide valve A313 to participate in the reaction, after the reaction is finished, the catalyst and reaction products enter a stripper 112 to finish the separation of oil gas and the catalyst, the oil gas upwards enters a stripping sedimentation vessel 109, after the catalyst with the particle size larger than 10-30 microns is filtered by a stripper filter 110, the oil gas leaves an oil gas outlet 111 at the top of the stripping sedimentation vessel 109 and enters a subsequent oil gas treatment unit. The spent catalyst enters the regenerator A208 and the regenerator B308 respectively through two spent catalyst supply pipes to finish the burning regeneration, and continuously enters each reactor through the corresponding regenerated catalyst supply pipes to participate in the reaction, thereby realizing the continuous cyclic reaction.
Examples:
the feeding amount of reactants is 1.3kg/h, a riser reactor is adopted as a reactor A and a reactor B, the two reactors are in an equal-diameter form, and a regenerator A is arranged; the reaction settler operating pressure 130kpa (gauge); the regeneration temperature is 700 ℃; the temperature of the regenerated catalyst entering the reactor A is 680 ℃, and the temperature of the regenerated catalyst entering the reactor B is 700 ℃;
The inner diameter of the reactor A is 15mm, and the length is 5000mm; the inner diameter of the reactor B is 10mm, the length of the reactor B is 3000mm, the inner diameter of the regenerator A is 60mm, and the height of the regenerator A is 3000mm; the inner diameter of the stripper is 60mm, and the height is 3000mm; the inner diameter of the regenerated catalyst supply pipe A is 15mm; the inner diameter of the regenerated catalyst supply pipe B is 12mm; the inner diameter of the catalyst supply pipe A for the spent catalyst is 15mm; the inner diameter of the spent catalyst conveying pipe A is 10mm, the outer diameter is 14mm, and the inner diameter of the cooling pipe is 20mm;
The outer sides of the two lifting pipes are all provided with heat insulation layers with the thickness of 10mm, and the heat conductivity coefficient of the heat insulation layer material is 0.1; the heat insulation layer is externally provided with an outer heat insulation and heat compensation heating furnace wire in three sections, the maximum power of each section is 1.8kw, and the use power is adjustable;
three sections of heating furnace wires are arranged outside the regenerator A, the maximum power of each section is 2.0kw, and the use power is adjustable; the stripper is provided with two sections of heating furnace wires, the maximum power of each section is 2.0kw, and the actual use power is adjustable; the two regenerated catalyst supply pipes are respectively provided with a section of heating furnace wire, the power is 2.0kw, and the actual use power is adjustable;
the heating wire is powered by 220 volts.
An 80mm thick heat insulation layer is arranged outside each device.
The stripping steam temperature is 350 ℃, and the steam quantity is 8g/min; the regenerator burns air for 20L/min;
in the embodiment, the whole material of the reactor is 316L, and the design temperature is 700 ℃; the regenerator material 310S, the design temperature is 800 ℃; the design pressure of the device is 0.6MPa.
Claims (8)
1.A catalyst continuous circulation reaction experimental device of double reactors,
Provided with a reactor A (103), a reactor B (403), a stripper (112), a regenerator A (208) and one or more regenerated catalyst supply pipes; the top of the stripper (112) is provided with a stripping sedimentation device (109), and the bottom of the stripper is provided with a spent catalyst supply pipe A (115); the top of the regenerator A (208) is provided with a regenerated sedimentation device A (205), and the bottom of the regenerator A is provided with a regenerated catalyst supply pipe A (211); the regenerated catalyst supply pipe A (211) is communicated with the reactor A (103), the outlet of the reactor A (103) is communicated with the stripper (112) or the stripping settler (109), and the outlet of the reactor B (403) is communicated with the stripper (112) or the stripping settler (109);
The method is characterized in that:
The device is provided with a spent catalyst conveying pipe A (202), wherein the inlet of the spent catalyst conveying pipe A (202) is communicated with a spent catalyst supply pipe A (115), the outlet of the spent catalyst conveying pipe A is communicated with a regenerator A (208) or a regeneration settler A (205), and a reactor B (403) is communicated with the bottom of the regenerator A (208) through a regenerated catalyst supply pipe B (311), so that continuous circulation of catalyst among the reactor A (103), the reactor B (403) and the regenerator A (208) is realized; a catalyst circulation amount metering unit A (203) is arranged on a spent catalyst conveying pipe A (202);
A heating furnace, a heat insulation and heat compensation heating furnace or a heat preservation layer is arranged outside the reactor A (103), the reactor B (403), the stripper (112), the spent catalyst supply pipe A (115), the regenerator A (208) and each regenerated catalyst supply pipe;
The heating furnace is provided with a heating furnace wire (603) and an external heat preservation layer (605);
The heat insulation and heat compensation heating furnace is provided with an inner heat insulation layer (602), heating furnace wires (603) and an outer heat preservation layer (605);
The temperature controller comprises a temperature thermocouple and a heating furnace wire power controller; the power controller is arranged on the heating furnace wire circuit.
2. The double-reactor catalyst continuous cycle reaction experimental device according to claim 1, characterized in that: heating furnaces are arranged outside the regenerator A (208) and the regenerated catalyst supply pipes or are arranged in sections, so that heat is supplied to the catalyst in the regenerator A (208) and the regenerated catalyst supply pipes respectively; temperature thermocouples are provided or staged inside and outside of the regenerator a (208) and the regenerated catalyst feed pipe, respectively.
3. The double-reactor catalyst continuous cycle reaction experimental device according to claim 1, characterized in that: an insulating and complementary heating furnace is arranged or sectionally arranged outside the outer walls of the reactor A (103) and the reactor B (403), and meanwhile, temperature thermocouples are arranged or sectionally arranged in the corresponding reactor and the region of the heating furnace wire (603) outside the reactor.
4. The double-reactor catalyst continuous cycle reaction experimental device according to claim 1, characterized in that: the reactor A (103) and/or the reactor B (403) are/is designed into a sectional detachable structure, and each reaction section realizes sectional detachment and replacement of the reactor through flanges or threads; the diameters of the reaction sections are the same or different.
5. The double-reactor catalyst continuous cycle reaction experimental device according to claim 1, characterized in that:
A regenerator B (308) is arranged, the regenerator B (308) is provided with a regeneration settler B (305), and the bottom of the stripper (112) is provided with a spent catalyst supply pipe B (117);
The reactor B (403) is communicated with the bottom of the regenerator B (308) through a regenerated catalyst supply pipe B (311); the inlet of the spent catalyst conveying pipe B (302) is communicated with the spent catalyst supply pipe B (117), and the outlet is communicated with the regenerator B (308) or the regeneration settler B (305), so that continuous circulation of the catalyst among the reactor A (103), the reactor B (403), the regenerator A (208) and the regenerator B (308) is realized; a catalyst circulation amount metering unit B (303) is arranged on a spent catalyst conveying pipe B (302);
an insulating layer or a heating furnace is arranged outside the regenerator B (308) and the spent catalyst supply pipe B (117).
6. The double-reactor catalyst continuous circulation reaction experimental device according to claim 1 or 5, characterized in that:
The catalyst circulation metering unit A (203) or the catalyst circulation metering unit B (303) comprises cooling pipes (508) which are correspondingly arranged outside the spent catalyst conveying pipe A (202) or the spent catalyst conveying pipe B (302), the cooling pipes (508) and the spent catalyst conveying pipe A (202) or the spent catalyst conveying pipe B (302) form an inner sleeve pipe or a ring pipe structure, and an annular gap between the cooling pipes (508) and the spent catalyst conveying pipe A (202) or the spent catalyst conveying pipe B (302) forms a cooling medium channel; a cooling medium inlet pipe (504) and a cooling medium outlet pipe (505) are respectively arranged at two ends of the cooling pipe (508); an insulation layer (509) is arranged outside the cooling pipe (508);
An inlet catalyst temperature thermocouple (502) and an outlet catalyst temperature thermocouple (503) are arranged on a spent catalyst conveying pipe A (202) or a spent catalyst conveying pipe B (302), and the inlet catalyst temperature thermocouple (502) and the outlet catalyst temperature thermocouple (503) are respectively positioned at the bottom end and the top end of a cooling pipe (508); a cooling medium outlet temperature thermocouple (507) is provided at the bottom end of the cooling pipe (508) or the cooling medium outlet pipe (505), and a cooling medium inlet temperature thermocouple (506) is provided at the top end of the cooling pipe (508) or the cooling medium inlet pipe (504).
7. The double-reactor catalyst continuous circulation reaction experimental device according to claim 1 or 5, characterized in that:
the reactor A (103) and/or the reactor B (403) are provided with one or more catalyst inlets, and the regenerator A (208) and/or the regenerator B (308) are provided with corresponding regenerated catalyst supply pipes, so that the regenerator A (208) and/or the regenerator B (308) can supply catalyst to the reactor A (103) and/or the reactor B (403) through the regenerated catalyst supply pipes through the catalyst inlets.
8. The double-reactor catalyst continuous circulation reaction experimental device according to claim 1 or 5, characterized in that: the regeneration temperature and the amount of intake air or the amount of oxygen in the gas of the regenerator A (208) or the regenerator B (308) are controlled to control the carbon content of the catalyst entering the reactor A (103) and/or the reactor B (403), and the temperature of the catalyst in the regenerated catalyst supply pipe A (211) and the regenerated catalyst supply pipe B (311) is controlled to control the temperature of the catalyst entering the reactor A (103) and/or the reactor B (403).
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