CN104140843A - Fluidized bed catalytic cracking tester - Google Patents
Fluidized bed catalytic cracking tester Download PDFInfo
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- CN104140843A CN104140843A CN201310177823.7A CN201310177823A CN104140843A CN 104140843 A CN104140843 A CN 104140843A CN 201310177823 A CN201310177823 A CN 201310177823A CN 104140843 A CN104140843 A CN 104140843A
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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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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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
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Abstract
The invention discloses a fluidized bed catalytic cracking tester to overcome problems caused by the phenomena that a conventional tester can limitedly change reaction time of raw oil in a riser reactor or downer reactor and reaction time is short. The fluidized bed catalytic cracking tester is provided with a reactor, a stripping device (18), a regenerator, a to-be-regenerated catalyst delivery pipe and a regenerated catalyst delivery pipe. The reactor is a bed type fluidized bed reactor (50); and the shell of the reactor is formed by a cylindrical upper reactor barrel (11), a lower reactor barrel (12) and an inverted circular table top like barrel. The outlet of the regenerated catalyst delivery pipe is located in the upper reactor barrel and faces downwards. A feed atomizing nozzle (13) is arranged at the bottom of the lower reactor barrel, and a nozzle outlet (130) faces upwards. The stripping device is arranged below the lower reactor barrel. The fluidized bed catalytic cracking tester is mainly used for laboratory investigation of catalytic cracking process for high-yield low-carbon gaseous olefins.
Description
Technical field
The present invention relates to petroleum chemical industry a kind of fluid catalystic cracking testing apparatus used.
Background technology
In recent years, application and the demand of low-carbon (LC) gas alkene (propylene and ethene) increase rapidly, and especially the rate of increase of propylene continues the rate of increase higher than ethene.Therefore, how making full use of on the basis of existing resource as early as possible the throughput of enlargement gas alkene efficiently, the important topic in face of Shi Bai petroleum chemical enterprise.Fluid catalytic cracking (FCC) is of paramount importance secondary processing means in petroleum refining industry; On the basis of FCC technique, developed the technique of some voluminous low-carbon (LC) gas alkene.In order further improving, to use catalyst cracking method by the technique of petroleum oil preparing gas alkene, just need to use corresponding catalytic cracking test device to study.
About catalytic cracking test device, external exploitation early have U.S. Atlantic Richfield company, the U.S. Davison of a Grace company Division of Chemistry.At home, some scientific research institutions have also built small riser catalytic cracking test device, as the XTL-3 type of Luoyang Engineering Co., Ltd of China Petrochemical Industry and XTL-5 type riser catalytic cracking test device.XTL equipment series, its stock oil oil inlet quantity is 1～1.5 kg/hr, the settling vessel of reaction-regeneration system and revivifier height are placed side by side.Riser tube is relatively short, is only provided with bottom feed nozzle, thereby changes the reaction times by changing the water vapor amount change oil gas linear speed of oil inlet quantity or injection, to the change in reaction times very limited (can only change in the scope in several seconds).The disclosed a kind of circulating fluidized bed reaction regeneration device of Chinese patent CN201997317U, comprises riser reactor, stripper, revivifier, reclaimable catalyst transfer limes, regenerated catalyst transfer limes, in its outside, is coated with resistance wire.This device is mainly used in carrying out the experimental study of conventional riser catalytic cracking.The disclosed a kind of catalytic cracking test device of CN202754958U, comprise that riser tube burns device, regenerated catalyst storage tank, descending-bed reactor, reacting-settler and stripper etc., be mainly used in carrying out the catalytic cracking process experimental study of finish short contact down-flow fluidized bed using ECT and the research of tubular type scorch test.Catalytic cracking process research by the fluid catalystic cracking testing apparatus of existing riser reactor or descending-bed reactor type for voluminous low-carbon (LC) gas alkene, subject matter is very limited to the change in stock oil reaction times in riser reactor or descending-bed reactor, reaction times shorter (conventionally can only be controlled at 2～3 seconds) in addition, the reaction depth that makes stock oil not, transformation efficiency is lower.This has all affected the evaluation to stock oil, catalyzer, reaction conditions.
Catalytic cracking process research for voluminous low-carbon (LC) gas alkene, also has static catalytic cracking testing apparatus; Its subject matter be catalyst levels less, can only periodical operation, can not simulate industrial continuous operation.In addition, catalyst regeneration device is not set, after each test, needing, with manually outwelling reacted old catalyzer the new catalyzer that changes the outfit, has increased labor capacity.
Summary of the invention
The object of this invention is to provide a kind of fluid catalystic cracking testing apparatus, to solve, the existing change to stock oil reaction times in riser reactor or descending-bed reactor of existing fluid catalystic cracking testing apparatus is limited, the shorter problem being caused of reaction times.
For addressing the above problem, the technical solution used in the present invention is: a kind of fluid catalystic cracking testing apparatus, be provided with reactor, stripper, revivifier, reclaimable catalyst transfer lime, regenerated catalyst, their outside surface is all coated with an electric heating element, reclaimable catalyst transfer lime is located between stripper and revivifier, regenerated catalyst is located between revivifier and reactor, the bottom of reactor is provided with atomizing feed nozzle, in stripper, be provided with stripping gas sparger, it is characterized in that: reactor is bed formula fluidized-bed reactor, its housing is by columnar reactor top cylindrical shell, reactor lower part cylindrical shell and the inverted round table face shape cylindrical shell being positioned between the two form, the outlet of regenerated catalyst is positioned at reactor top cylindrical shell, outlet downwards, atomizing feed nozzle is located at the bottom of reactor lower part cylindrical shell, jet exit upwards, the top of reactor top cylindrical shell is provided with blind flange, blind flange is provided with reaction oil gas strainer and reaction oil tracheae, stripper is located at the below of reactor lower part cylindrical shell, the housing of stripper is cylindrical drum.
The present invention uses bed formula fluidized-bed reactor; In process of the test, regenerated catalyst flows from top to bottom, and atomized feed oil flows from bottom to top, and in dense-phase catalyst reaction bed, counter current contact is carried out catalytic cracking reaction.Detailed process of the test, is shown in the explanation of this specification sheets embodiment part.Adopt the present invention, there is following beneficial effect: (1) is by regulating the size of stock oil oil inlet quantity or atomizing steam amount to change the weight space velocity of catalytic cracking reaction, can be with comparalive ease the reaction times of feed change oil in bed formula fluidized-bed reactor in the larger context, reaction times is also long, thereby can make stock oil reach enough reaction depth, raising transformation efficiencys.The variation range in reaction times and the length in reaction times, can reflect by the weight space velocity (it is reciprocal is the reaction times) in test conditions of the present invention.(2), in dense-phase catalyst reaction bed, atomized feed oil and regenerated catalyst counter current contact, can make feedstock fully contact with all granules of catalyst.In the process of stock oil generation catalytic cracking reaction, crackate can continue to contact and react with the granules of catalyst flowing downward, and produces micromolecular gas alkene, thereby improves the productive rate of low-carbon (LC) gas alkene.
The present invention is mainly used in the laboratory study of the catalytic cracking process of voluminous low-carbon (LC) gas alkene.Use the present invention, can carry out cracking performance and products thereof the investigation of character of various stock oils, the experimental study of the evaluation of catalyzer, reaction-regeneration kinetics aspect.Fluid catalystic cracking testing apparatus with respect to existing riser reactor or descending-bed reactor type, the present invention can complete its research work that cannot carry out, stock oil, catalyzer, reaction conditions are made to better evaluation, for the design of full scale plant, produce reliable basic data is provided.Use the present invention, carry out under the same conditions the resulting data of test of many times and there is good repeatability; Reaction-regenerative process can be carried out by continuous circulation, effectively overcomes the shortcoming that existing static catalytic cracking testing apparatus exists.
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.The drawings and specific embodiments do not limit the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the structure and layout schematic diagram of a kind of fluid catalystic cracking testing apparatus of the present invention, and bed formula fluidized-bed reactor and bed formula fluid bed regenerator are set up in parallel with height.
Fig. 2 is the structure and layout schematic diagram of another kind of fluid catalystic cracking testing apparatus of the present invention, and bed formula fluidized-bed reactor and bed formula fluid bed regenerator are just set up in parallel.
Fig. 3 is the structural representation of the present invention's a kind of plug valve of regenerating used.
In Fig. 1 to Fig. 3, same reference numerals represents identical technical characterictic.
Embodiment
Referring to Fig. 1 and Fig. 2, fluid catalystic cracking testing apparatus of the present invention (referred to as testing apparatus), be provided with reactor, stripper 18, revivifier, reclaimable catalyst transfer lime, regenerated catalyst, their outside surface is all coated with an electric heating element.Reclaimable catalyst transfer lime is located between stripper 18 and revivifier, and regenerated catalyst is located between revivifier and reactor.The bottom of reactor is provided with atomizing feed nozzle 13, is provided with stripping gas sparger 19 in stripper 18.The present invention, reactor is bed formula fluidized-bed reactor 50, and its housing is comprised of columnar reactor top cylindrical shell 11, reactor lower part cylindrical shell 12 and the inverted round table face shape cylindrical shell that is positioned between the two, and these cylindrical shells coaxially arrange.The outlet of regenerated catalyst is positioned at reactor top cylindrical shell 11, and outlet downwards.Atomizing feed nozzle 13 is located at the bottom of reactor lower part cylindrical shell 12, and jet exit 130 upwards.The outlet of regenerated catalyst and jet exit 130 are all positioned on the axial line of bed formula fluidized-bed reactor 50.The top of reactor top cylindrical shell 11 is provided with blind flange, and blind flange is provided with reaction oil gas strainer 34 and reaction oil tracheae.Reaction oil gas strainer 34 arranges a plurality of (3～10 of operated by rotary motion), and each oil gas filter 34 is connected with a reaction oil gas arm.Each root reaction oil gas arm is connected with a reaction oil gas house steward 28, and reaction oil gas house steward 28 outlet is reclaimed with oil gas product metering, analytical system is connected (figure slightly).Stripper 18 is located at the below of reactor lower part cylindrical shell 12.The housing of stripper 18 is cylindrical drum, and its top is connected with the bottom of reactor lower part cylindrical shell 12 by an inverted round table face shape cylindrical shell, and bottom is connected with the entrance of reclaimable catalyst transfer lime.Described stripping gas sparger 19 is located at the bottom of stripper 18 cylindrical drums.
The present invention, revivifier is used bed formula fluid bed regenerator 60.The housing of bed formula fluid bed regenerator 60 is comprised of columnar revivifier top cylindrical shell 1, revivifier bottom cylindrical shell 2 and the inverted round table face shape cylindrical shell that is positioned between the two, and these cylindrical shells coaxially arrange.The bottom of revivifier bottom cylindrical shell 2 is provided with main air distributor 3; The outlet of reclaimable catalyst transfer lime is positioned at revivifier top cylindrical shell 1, and outlet downwards.The entrance of regenerated catalyst is connected with the bottom of revivifier bottom cylindrical shell 2 by an inverted round table face shape cylindrical shell.The top of revivifier top cylindrical shell 1 is provided with blind flange, and blind flange is provided with regenerated flue gas strainer 33, regenerated flue gas pipe, catalyst addition tube 30, and catalyst addition tube 30 is provided with catalyzer charging valve 29.Smoke filter 33 arranges a plurality of (3～10 of operated by rotary motion), and each smoke filter 33 is connected with a root regeneration flue gas arm.Each root regeneration flue gas arm is connected with a root regeneration flue gas house steward 27, and regenerated flue gas house steward 27 outlet is cooling with flue gas and control metering system be connected (figure summary).
Referring to Fig. 1 and Fig. 2, described reclaimable catalyst transfer lime, by the direction from stripper 18 to bed formula fluid bed regenerator 60, is comprised of inclined tube 22 to be generated, spent riser 25 and reclaimable catalyst outlet pipe 26 successively.Inclined tube 22 to be generated is connected by plug valve 24 to be generated with spent riser 25, and (opening for feed of plug valve 24 to be generated is connected with the outlet at bottom of inclined tube 22 to be generated, and discharge port is connected with the bottom inlet of spent riser 25; Described connection generally adopts welding, spherical joint to connect or flange connects), inclined tube 22 to be generated is provided with reclaimable catalyst sampling valve 31.Described regenerated catalyst, by the direction from bed formula fluid bed regenerator 60 to bed formula fluidized-bed reactor 50, is comprised of standpipe 5, regenerator sloped tube 6, regenerated catalyst riser tube 9, regenerated catalyst outlet pipe 10 successively.Regenerator sloped tube 6 is connected by regeneration plug valve 8 with regenerated catalyst riser tube 9, and (opening for feed of regeneration plug valve 8 is connected with the outlet at bottom of regenerator sloped tube 6, and discharge port is connected with the bottom inlet of regenerated catalyst riser tube 9; Described connection generally adopts welding, spherical joint to connect or flange connects), regenerator sloped tube 6 is provided with regenerated catalyst sampling valve 32.The entrance of inclined tube 22 to be generated is the entrance of reclaimable catalyst transfer lime, the outlet of reclaimable catalyst outlet pipe 26 is the outlet of reclaimable catalyst transfer lime, the entrance of standpipe 5 is the entrance of regenerated catalyst, and the outlet 100 of regenerated catalyst outlet pipe 10 is the outlet of regenerated catalyst.Inclined tube 22 to be generated and regenerator sloped tube 6 angle of inclination with respect to the horizontal plane, should be greater than the slope of repose of catalyzer.
The top of regenerated catalyst riser tube 9 is provided with the first pressure tap 38, and bottom is provided with the second pressure tap 39; The top of bed formula fluidized-bed reactor 50 is provided with the 3rd pressure tap 40, and the bottom of stripper 18 is provided with the 4th pressure tap 41.Each pressure tap is equipped with pressure measuring instruments to measure pressure everywhere.
Atomizing feed nozzle 13 is connected with atomizing steam pipe 15 with raw material oil pipe 14.The other end of raw material oil pipe 14 is connected with fuel oil preheating stove 16, and the other end of atomizing steam pipe 15 is connected with atomization steam boiler 17.Stripping gas sparger 19 is connected with stripping gas pipe 20, and the other end of stripping gas pipe 20 is connected with stripping gas stove 21.
Testing apparatus of the present invention, bed formula fluidized-bed reactor 50 can be set up in parallel with height (as shown in Figure 1) with bed formula fluid bed regenerator 60 or height is set up in parallel (as shown in Figure 2).
Referring to Fig. 1 and Fig. 2, some main structure parameters of testing apparatus of the present invention are generally as follows: the diameter of regenerated catalyst riser tube 9 is 10～30 millimeters, and height n is 3～18 meters; The diameter of spent riser 25 is 10～30 millimeters, and height m is 3～16 meters.The diameter C of reactor top cylindrical shell 11 is 1.5～5 times of reactor lower part cylindrical shell 12 diameter D, and height t is 0.3～0.6 meter; The diameter D of reactor lower part cylindrical shell 12 is 3～8 times of regenerated catalyst riser tube 9 diameters, and height s is 3～10 times of reactor top cylindrical shell 11 height t.The diameter M of stripper 18 cylindrical shells is 0.2～0.8 times of reactor lower part cylindrical shell 12 diameter D, and height k is 3～10 times of reactor top cylindrical shell 11 height t.The diameter A of revivifier top cylindrical shell 1 is 1～1.3 times of reactor top cylindrical shell 11 diameter C, and height h is 0.3～0.6 meter; The diameter B of revivifier bottom cylindrical shell 2 is 0.2～0.7 times of revivifier top cylindrical shell 1 diameter A, and height e is 3～10 times of revivifier top cylindrical shell 1 height h.The diameter of various cylindrical shell of the present invention and pipeline, all refers to its interior diameter.
In testing apparatus of the present invention, cylindrical shell and the various pipeline of the cylindrical shell of bed formula fluidized-bed reactor 50 and bed formula fluid bed regenerator 60, blind flange, stripper 18, all adopt stainless material.Except explanation, relevant connection all adopts welding.The outside surface of bed formula fluidized-bed reactor 50, bed formula fluid bed regenerator 60, stripper 18 and various pipelines is all coated with an electric heating element, and (figure slightly; Pipeline section, reclaimable catalyst outlet pipe 26 that regenerated catalyst outlet pipe 10 is positioned within reactor top cylindrical shell 11 are positioned at except the pipeline section within revivifier top cylindrical shell 1), an electric heating element can be conventional resistance wire or with tile of resistance wire etc.The parts such as the present invention's various valves used, atomizing feed nozzle 13, fuel oil preheating stove 16, atomization steam boiler 17, stripping gas stove 21, stripping gas sparger 19, main air distributor 3, can be used fluid catalystic cracking experimental technique field to be commonly used.Fuel oil preheating stove 16, atomization steam boiler 17, the general electrical heater that uses of stripping gas stove 21, atomizing feed nozzle 13 can be used the catalytic cracking atomizing feeding nozzle described in CN202148288U.Reaction oil gas strainer 34 and regenerated flue gas strainer 33 can use conventional pottery or metallic filter.
Regeneration plug valve 8 and plug valve to be generated 24 can request for utilization number be the plug valve described in 201220592166.3 Chinese patent.Shown in Fig. 3, this plug valve is as regeneration plug valve 8; Reference numeral 81 in Fig. 3 represents valve rod, and 82 represent valve cone, and 83 represent valve body, and 84 represent valve rod end, and 85 represent plug valve cavity, and 86 represent opening for feed, and 87 represent discharge port, and 88 represent loosening airduct, and 89 represent loosening wind, and 90 represent lift gas pipe.Valve rod end 84 is connected with electric operator (figure slightly), and electric operator can be bought.The general nitrogen that uses of loosening wind 89.When the plug valve described in above patent is used as plug valve 24 to be generated, as long as change the regenerated catalyst riser tube 9 in Fig. 3 into spent riser 25, regenerator sloped tube 6, change inclined tube 22 to be generated, regenerated catalyst into and promote gas 7 (nitrogen) and change that reclaimable catalyst promotes gas 23 (air), loosening wind 89 changes air into by nitrogen and changes the vergence direction of plug valve into, figure omits.Except the plug valve described in above patent, other plug valve that meets requirement of the present invention also can be used.
Below in conjunction with Fig. 1 and Fig. 2, the process of using testing apparatus of the present invention to test is described.Stock oil 140 is preheated by raw material oil pipe 14 and enters atomizing feed nozzle 13 in fuel oil preheating stove 16, and water 150 is heated, forms atomizing steam and enters atomizing feed nozzle 13 by atomizing steam pipe 15 in atomization steam boiler 17.Stock oil is atomized steam atomizing by upwards ejection of jet exit 130, and regenerated catalyst flows out downwards through the outlet 100 of regenerated catalyst outlet pipe 10 simultaneously.In the dense-phase catalyst reaction bed of bed formula fluidized-bed reactor 50 bottoms, above-mentioned atomized feed oil carries out catalytic cracking reaction with regenerated catalyst counter current contact.The oil gas generating after reaction upwards flows into the dilute phase section on bed formula fluidized-bed reactor 50 tops, together with the regenerated catalyst that enters this dilute phase section, promote the oil gas that gas 7 and the stripping gas after the interior stripping reclaimable catalyst of stripper 18 and stripping go out, after reaction oil gas strainer 34 filters out catalyzer, enter each root reaction oil gas arm, finally by reaction oil gas house steward 28, enter oil gas product metering recovery, analytical system (figure summary; By this system, can be obtained the distributed data of ethene, propylene and other products).In Fig. 1 and Fig. 2, Reference numeral 37 represents dense-phase catalyst reaction bed interface; The below at this interface is dense-phase catalyst reaction bed (being positioned at reactor lower part cylindrical shell 12), and top is the dilute phase section of bed formula fluidized-bed reactor 50.In dense-phase catalyst reaction bed, participate in after reaction, the reclaimable catalyst of having tied charcoal flows into stripper 18 downwards.Water or nitrogen 200 become stripping gas (wherein water becomes water vapor) after being heated in stripping gas stove 21, through stripping gas pipe 20, stripping gas sparger 19, enter stripper 18.In stripper 18, stripping gas upwards flows, and the reclaimable catalyst flowing downward is carried out to stripping, and stripping goes out reclaimable catalyst entrained oil gas.Reclaimable catalyst after stripping is flowed out by the bottom of stripper 18, enters the top of bed formula fluid bed regenerator 60 through inclined tube 22 to be generated, plug valve to be generated 24, spent riser 25 and reclaimable catalyst outlet pipe 26.In said process, through the plug valve cavity of plug valve 24 to be generated, to the bottom of spent riser 25, pass into reclaimable catalyst and promote gas 23 (being generally air), to promote the reclaimable catalyst in spent riser 25.
The reclaimable catalyst being entered in bed formula fluid bed regenerator 60 by reclaimable catalyst outlet pipe 26 flows downward.Main air 4 (being generally air) enters bed formula fluid bed regenerator 60 through main air distributor 3, upwards flows.In the dense-phase catalyst regenerator bed of bed formula fluid bed regenerator 60 bottoms, above-mentioned reclaimable catalyst and main air 4 counter current contact, the coke on reclaimable catalyst is by burning-off, and activation recovering, becomes regenerated catalyst.The flue gas generating after regenerative response upwards flows into the dilute phase section on bed formula fluid bed regenerator 60 tops, together with the reclaimable catalyst that enters this dilute phase section, promote gas 23 (also burn and become flue gas while using air), after regenerated flue gas strainer 33 filters out catalyzer, enter each root regeneration flue gas arm, finally by regenerated flue gas house steward 27, enter flue gas cooling and control metering system (figure slightly).In Fig. 1 and Fig. 2, Reference numeral 36 represents dense-phase catalyst regenerator bed interface; The below at this interface is dense-phase catalyst regenerator bed, and top is the dilute phase section of bed formula fluid bed regenerator 60.Regenerated catalyst in dense-phase catalyst regenerator bed after regeneration flows downward, flow out bottom by bed formula fluid bed regenerator 60, the top that enters bed formula fluidized-bed reactor 50 through standpipe 5, regenerator sloped tube 6, regeneration plug valve 8, regenerated catalyst riser tube 9, regenerated catalyst outlet pipe 10, participates in catalytic cracking reaction again.In said process, through the plug valve cavity of regeneration plug valve 8, to the bottom of regenerated catalyst riser tube 9, pass into regenerated catalyst and promote gas 7 (being generally nitrogen), to promote the regenerated catalyst in regenerated catalyst riser tube 9.
Some main experimental conditions of testing apparatus of the present invention are generally as follows.The catalyst inventory of full device is 2～20 kilograms, and the oil inlet quantity of stock oil 140 is 1～15 kg/hr, and atomizing steam amount is 0.12～3 kg/hr.In bed formula fluidized-bed reactor 50, catalytic cracking reaction temperature is 400～700 ℃, and reaction pressure is 0.01～0.2MPa (pressure that the present invention mentions is gauge pressure), and agent-oil ratio is 4～12, and weight space velocity is 0.5～50 hour
-1(weight space velocity is preferably 15～30 hours
-1).Above-mentioned temperature of reaction above jet exit 130 200～300 millimeters locate to measure, reaction pressure is in the measurement of the top (i.e. the 3rd pressure tap 40 places) of bed formula fluidized-bed reactor 50; Agent-oil ratio for by the outlet 100 of regenerated catalyst outlet pipe 10 enter the regenerated catalyst in bed formula fluidized-bed reactor 50 weight rate (kg/hr) with by the jet exit 130 of atomizing feed nozzle 13 enter the atomized feed oil in bed formula fluidized-bed reactor 50 weight rate (kg/hr) ratio; (final unit is hour weight space velocity
-1), refer to by the jet exit 130 of atomizing feed nozzle 13 enter into the atomized feed oil in bed formula fluidized-bed reactor 50 flow (kg/hr) with bed formula fluidized-bed reactor 50 in catalyst inventory (kilogram) ratio.
In stripper 18, stripping temperature is 400～550 ℃; This temperature is measured at the middle part of the interior reclaimable catalyst bed height of stripper 18.In bed formula fluid bed regenerator 60, regeneration temperature is 600～800 ℃, and pressure is 0.01～0.2MPa; Regeneration temperature is the medial temperature of dense-phase catalyst regenerator bed, and pressure is measured at the top of bed formula fluid bed regenerator 60.
Stock oil 140 can be liquefied petroleum gas (LPG), gasoline, diesel oil, wax oil, residual oil etc.Temperature after stock oil 140 is preheated in fuel oil preheating stove 16 is 100～400 ℃.
Catalyzer can be the catalytic cracking catalyst (catalytic cracking catalyst of the trades mark such as MMC-2, CIP-1, RAG-7) of various voluminous low-carbon (LC) gas alkene.Before test, first the catalyzer 35 of test use is joined in bed formula fluid bed regenerator 60 through catalyst addition tube 30 and catalyzer charging valve 29.Through reclaimable catalyst sampling valve 31 and regenerated catalyst sampling valve 32, can to reclaimable catalyst and regenerated catalyst, carry out sampling analysis respectively, to determine its carbon content.
In process of the test, with differential pressure transmitter, measure the pressure reduction between the first pressure tap 38 and the second pressure tap 39, according to this pressure reduction and the difference of setting pressure reduction, regulate the aperture of regeneration plug valve 8, effectively the catalyst recirculation amount in Control experiment device.With differential pressure transmitter, measure the pressure reduction between the 3rd pressure tap 40 and the 4th pressure tap 41, according to this pressure reduction and the difference of setting pressure reduction, regulate the aperture of plug valve 24 to be generated, the height that can effectively control the interior dense-phase catalyst reaction bed of bed formula fluidized-bed reactor 50 interface 37, fully guarantees the catalytic cracking reaction effect in dense-phase catalyst reaction bed.Above-mentioned measurement, regulate process can automatically complete under the control of computer, and detailed description is omitted.
Use testing apparatus of the present invention, can carry out cracking performance and products thereof the investigation of character of various stock oils, the evaluation of catalyzer etc. meet multiple test objective requirement; Those skilled in the art can design various test subjects as required.
Such as, while evaluating a certain catalytic cracking catalyst, first select a kind of stock oil to test.Change respectively the principal reaction conditions such as catalytic cracking reaction temperature, reaction pressure, agent-oil ratio, weight space velocity and stock oil oil inlet quantity, research experiment, obtains the optimum reaction condition that this catalytic cracking catalyst and this stock oil can voluminous low-carbon (LC) gas alkene.Then stock oil is replaced by other different types of stock oil, the research experiment under various reaction conditionss that uses the same method, obtains the optimum reaction condition that this catalytic cracking catalyst and other stock oil can voluminous low-carbon (LC) gas alkene.
For another example, while evaluating the cracking performance of a certain stock oil, a kind of catalytic cracking catalyst of first-selected selection is tested.Change respectively the principal reaction conditions such as catalytic cracking reaction temperature, reaction pressure, agent-oil ratio, weight space velocity and stock oil oil inlet quantity, research experiment.Then by catalyst change, be other different types of catalytic cracking catalyst, research experiment under various reaction conditionss uses the same method.Finally by the contrast of each test-results, obtain a kind of be applicable to this kind of stock oil can voluminous low-carbon (LC) gas alkene optimum catalyst and optimum reaction conditions.
Claims (6)
1. a fluid catalystic cracking testing apparatus, be provided with reactor, stripper (18), revivifier, reclaimable catalyst transfer lime, regenerated catalyst, their outside surface is all coated with an electric heating element, reclaimable catalyst transfer lime is located between stripper (18) and revivifier, regenerated catalyst is located between revivifier and reactor, the bottom of reactor is provided with atomizing feed nozzle (13), in stripper (18), be provided with stripping gas sparger (19), it is characterized in that: reactor is bed formula fluidized-bed reactor (50), its housing is by columnar reactor top cylindrical shell (11), reactor lower part cylindrical shell (12) and the inverted round table face shape cylindrical shell being positioned between the two form, the outlet of regenerated catalyst is positioned at reactor top cylindrical shell (11), outlet downwards, atomizing feed nozzle (13) is located at the bottom of reactor lower part cylindrical shell (12), jet exit (130) upwards, the top of reactor top cylindrical shell (11) is provided with blind flange, blind flange is provided with reaction oil gas strainer (34) and reaction oil tracheae, stripper (18) is located at the below of reactor lower part cylindrical shell (12), the housing of stripper (18) is cylindrical drum.
2. testing apparatus according to claim 1, it is characterized in that: revivifier is bed formula fluid bed regenerator (60), its housing is by columnar revivifier top cylindrical shell (1), revivifier bottom cylindrical shell (2) and the inverted round table face shape cylindrical shell being positioned between the two form, the bottom of revivifier bottom cylindrical shell (2) is provided with main air distributor (3), the outlet of reclaimable catalyst transfer lime is positioned at revivifier top cylindrical shell (1), the entrance of regenerated catalyst is connected with the bottom of revivifier bottom cylindrical shell (2) by an inverted round table face shape cylindrical shell, the top of revivifier top cylindrical shell (1) is provided with blind flange, blind flange is provided with regenerated flue gas strainer (33), regenerated flue gas pipe, catalyst addition tube (30), catalyst addition tube (30) is provided with catalyzer charging valve (29).
3. testing apparatus according to claim 2, it is characterized in that: described reclaimable catalyst transfer lime is by the direction from stripper (18) to bed formula fluid bed regenerator (60), successively by inclined tube to be generated (22), spent riser (25) and reclaimable catalyst outlet pipe (26) form, inclined tube to be generated (22) is connected by plug valve to be generated (24) with spent riser (25), inclined tube to be generated (22) is provided with reclaimable catalyst sampling valve (31), described regenerated catalyst is by the direction from bed formula fluid bed regenerator (60) to bed formula fluidized-bed reactor (50), successively by standpipe (5), regenerator sloped tube (6), regenerated catalyst riser tube (9), regenerated catalyst outlet pipe (10) forms, regenerator sloped tube (6) is connected by regeneration plug valve (8) with regenerated catalyst riser tube (9), regenerator sloped tube (6) is provided with regenerated catalyst sampling valve (32), the top of regenerated catalyst riser tube (9) is provided with the first pressure tap (38), bottom is provided with the second pressure tap (39), the top of bed formula fluidized-bed reactor (50) is provided with the 3rd pressure tap (40), the bottom of stripper (18) is provided with the 4th pressure tap (41).
4. testing apparatus according to claim 3, it is characterized in that: atomizing feed nozzle (13) is connected with atomizing steam pipe (15) with raw material oil pipe (14), the other end of raw material oil pipe (14) is connected with fuel oil preheating stove (16), the other end of atomizing steam pipe (15) is connected with atomization steam boiler (17), stripping gas sparger (19) is connected with stripping gas pipe (20), and the other end of stripping gas pipe (20) is connected with stripping gas stove (21).
5. according to the testing apparatus described in claim 3 or 4, it is characterized in that: bed formula fluidized-bed reactor (50) is set up in parallel with height with bed formula fluid bed regenerator (60) or height is set up in parallel.
6. testing apparatus according to claim 5, it is characterized in that: the diameter of regenerated catalyst riser tube 9 is 10～30 millimeters, height n is 3～18 meters, the diameter of spent riser 25 is 10～30 millimeters, height m is 3～16 meters, the diameter C of reactor top cylindrical shell (11) is 1.5～5 times of reactor lower part cylindrical shell (12) diameter D, height t is 0.3～0.6 meter, the diameter D of reactor lower part cylindrical shell (12) is 3～8 times of regenerated catalyst riser tube (9) diameter, height s is 3～10 times of reactor top cylindrical shell (11) height t, the diameter M of stripper (18) cylindrical shell is 0.2～0.8 times of reactor lower part cylindrical shell (12) diameter D, height k is 3～10 times of reactor top cylindrical shell (11) height t, the diameter A of revivifier top cylindrical shell (1) is 1～1.3 times of reactor top cylindrical shell (11) diameter C, height h is 0.3～0.6 meter, the diameter B of revivifier bottom cylindrical shell (2) is 0.2～0.7 times of revivifier top cylindrical shell (1) diameter A, height e is 3～10 times of revivifier top cylindrical shell (1) height h.
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| CN104845661A (en) * | 2015-05-04 | 2015-08-19 | 中国石油大学(华东) | Catalytic cracking reactivator test simulation method and device |
| CN107990007A (en) * | 2017-12-07 | 2018-05-04 | 吉林省松原石油化工股份有限公司 | Fluidization up flow type multiple reactor is connected and the downflow system plug valve of regeneration technology |
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| CN201997317U (en) * | 2011-02-22 | 2011-10-05 | 中国石油天然气股份有限公司 | Reaction regeneration device of circulating fluidized bed |
| CN202148288U (en) * | 2011-07-27 | 2012-02-22 | 中国石油化工股份有限公司 | Catalytic cracking atomization feeding nozzle |
| CN202754958U (en) * | 2012-07-25 | 2013-02-27 | 中国石油化工集团公司 | Catalytic cracking testing apparatus |
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| CN201997317U (en) * | 2011-02-22 | 2011-10-05 | 中国石油天然气股份有限公司 | Reaction regeneration device of circulating fluidized bed |
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