CN104140843B - A kind of fluid catalystic cracking testing apparatus - Google Patents
A kind of fluid catalystic cracking testing apparatus Download PDFInfo
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- CN104140843B CN104140843B CN201310177823.7A CN201310177823A CN104140843B CN 104140843 B CN104140843 B CN 104140843B CN 201310177823 A CN201310177823 A CN 201310177823A CN 104140843 B CN104140843 B CN 104140843B
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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
Abstract
The invention discloses a kind of fluid catalystic cracking testing apparatus, to solve, reaction times shorter the caused problem limited to the change in stock oil reaction times in riser reactor or descending-bed reactor existing for existing testing apparatus.The present invention is provided with reactor, stripper (18), revivifier, reclaimable catalyst transfer lime, regenerated catalyst.Reactor is bed formula fluidized-bed reactor (50), and its housing is made up of columnar reactor top cylindrical shell (11), reactor lower part cylindrical shell (12) and the inverted round table face shape cylindrical shell be positioned between the two.The outlet of regenerated catalyst is positioned at reactor top cylindrical shell, and outlet downwards; Atomizing feed nozzle (13) is located at the bottom of reactor lower part cylindrical shell, and jet exit (130) upwards.Stripper is located at the below of reactor lower part cylindrical shell.The present invention is mainly used in the laboratory study of the catalytic cracking process of voluminous low-carbon (LC) gaseous olefin.
Description
Technical field
The present invention relates to a kind of fluid catalystic cracking testing apparatus that petroleum chemical industry is used.
Background technology
In recent years, application and the demand of low-carbon (LC) gaseous olefin (propylene and ethene) increase rapidly, and especially the rate of increase of propylene continues the rate of increase higher than ethene.Therefore, how the throughput of enlargement gas alkene efficiently as early as possible on the basis making full use of existing resource, is the important topic of pendulum in face of petroleum chemical enterprise.Fluid catalytic cracking (FCC) is of paramount importance secondary processing means in petroleum refining industry; On the basis of FCC technique, have developed the technique of some voluminous low-carbon (LC) gaseous olefin.In order to improve the technique using catalyst cracking method by petroleum oil preparing gas alkene further, just need to use corresponding catalytic cracking test device to study.
About catalytic cracking test device, external exploitation comparatively early have AtlanticRichfield company of the U.S., U.S. Grace company Davison Division of Chemistry.At home, some scientific research institutions have also built small riser catalytic cracking test device, as XTL-3 type and the XTL-5 type riser catalytic cracking test device of Sinopec Luoyang Petrochemical Engineering Corporation.XTL equipment series, its stock oil oil inlet quantity is 1 ~ 1.5 kg/hr, and 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, by changing the water vapor amount of oil inlet quantity or injection thus changing oil gas linear speed and change the reaction times, to the change in reaction times very limited (can only change in the scope in a few second).Disclosed in Chinese patent CN201997317U, a kind of circulating fluidized bed reaction regeneration device, comprises riser reactor, stripper, revivifier, reclaimable catalyst transfer limes, regenerated catalyst transfer limes, is coated with resistance wire in its outside.This device is mainly used in the experimental study carrying out Conventional riser catalytic cracking.A kind of catalytic cracking test device disclosed in CN202754958U, comprise riser tube and burn 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.The fluid catalystic cracking testing apparatus of existing riser reactor or descending-bed reactor type is used for the catalytic cracking process research of voluminous low-carbon (LC) gaseous olefin, subject matter is very limited to the change in stock oil reaction times in riser reactor or descending-bed reactor, reaction times shorter (usually can only control at 2 ~ 3 seconds) in addition, make the reaction depth of stock oil not, transformation efficiency is lower.This all have impact on the evaluation to stock oil, catalyzer, reaction conditions.
Catalytic cracking process for voluminous low-carbon (LC) gaseous olefin is studied, and also has static catalytic cracking testing apparatus; Its subject matter be catalyst levels less, can only periodical operation, industrial continuous operation can not be simulated.In addition, catalyst regeneration device not being set, needing after each test, with manually outwelling reacted old catalyzer and the new catalyzer that changes the outfit, to add labor capacity.
Summary of the invention
The object of this invention is to provide a kind of fluid catalystic cracking testing apparatus, to solve, reaction times shorter the caused problem limited to the change in stock oil reaction times in riser reactor or descending-bed reactor existing for existing fluid catalystic cracking testing apparatus.
For solving the 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, stripping gas distributor is provided with in stripper, 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 composition be positioned between the two, 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 carries 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) changes the weight space velocity of catalytic cracking reaction by regulating the size of stock oil oil inlet quantity or atomizing steam amount, can the feed change reaction times of oil in bed formula fluidized-bed reactor in the larger context with comparalive ease, reaction times is also long, thus the reaction depth that stock oil can be made to reach enough, raising transformation efficiency.The variation range in reaction times and the length in reaction times, can be reflected 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 with the granules of catalyst flowed downward to react, and produces micromolecular gaseous olefin, thus improves the productive rate of low-carbon (LC) gaseous olefin.
The present invention is mainly used in the laboratory study of the catalytic cracking process of voluminous low-carbon (LC) gaseous olefin.Use the present invention, the investigation of the cracking performance of various stock oil and products thereof character, the evaluation of catalyzer, the experimental study of reaction-regeneration kinetics aspect can be carried out.Relative to the fluid catalystic cracking testing apparatus of existing riser reactor or descending-bed reactor type, the present invention can complete its research work that cannot carry out, better evaluation is made to stock oil, catalyzer, reaction conditions, for full scale plant design, produce reliable basic data is provided.Use the present invention, carry out the data that test of many times obtains under the same conditions 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 of a kind of fluid catalystic cracking testing apparatus of the present invention and layout schematic diagram, and bed formula fluidized-bed reactor and bed formula fluid bed regenerator are set up in parallel with height.
Fig. 2 is the structure of another kind of fluid catalystic cracking testing apparatus of the present invention and layout schematic diagram, and bed formula fluidized-bed reactor and bed formula fluid bed regenerator height are set up in parallel.
Fig. 3 is the present invention's a kind of structural representation regenerating plug valve used.
In Fig. 1 to Fig. 3, same reference numerals represents identical technical characteristic.
Embodiment
See Fig. 1 and Fig. 2, fluid catalystic cracking testing apparatus (referred to as testing apparatus) of the present invention, 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 distributor 19 in stripper 18.The present invention, reactor is bed formula fluidized-bed reactor 50, and its housing is made up of columnar reactor top cylindrical shell 11, reactor lower part cylindrical shell 12 and the inverted round table face shape cylindrical shell be positioned between the two, and these cylindrical shells are coaxially arranged.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 is arranged multiple (generally arranging 3 ~ 10), and each oil gas filter 34 is connected with a reaction oil gas arm.Each reaction oil gas arm is connected with a reaction oil gas house steward 28, the outlet of reaction oil gas house steward 28 measure with oil gas product reclaim, analytical system is connected (scheme 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 distributor 19 is located at the bottom of stripper 18 cylindrical drum.
The present invention, revivifier uses bed formula fluid bed regenerator 60.The housing of bed formula fluid bed regenerator 60 is made up of columnar revivifier top cylindrical shell 1, revivifier lower cylinder 2 and the inverted round table face shape cylindrical shell be positioned between the two, and these cylindrical shells are coaxially arranged.The bottom of revivifier lower cylinder 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 lower cylinder 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 is arranged multiple (generally arranging 3 ~ 10), 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 the outlet of regenerated flue gas house steward 27 cools and controls metering system and is connected (scheming slightly) with flue gas.
See Fig. 1 and Fig. 2, described reclaimable catalyst transfer lime, by from stripper 18 to the direction of bed formula fluid bed regenerator 60, is made up of inclined tube 22 to be generated, spent riser 25 and reclaimable catalyst outlet pipe 26 successively.Inclined tube 22 to be generated and spent riser 25 are connected by plug valve 24 to be generated, 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 connection or Flange joint), inclined tube 22 to be generated is provided with reclaimable catalyst sampling valve 31.Described regenerated catalyst, by from bed formula fluid bed regenerator 60 to the direction of bed formula fluidized-bed reactor 50, is made up of standpipe 5, regenerator sloped tube 6, regenerated catalyst riser tube 9, regenerated catalyst outlet pipe 10 successively.By regenerating plug valve 8, regenerator sloped tube 6 and regenerated catalyst riser tube 9 are connected that (opening for feed regenerating 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 connection or Flange joint), regenerator sloped tube 6 is provided with regenerated catalyst sampling valve 32.The entrance of inclined tube 22 to be generated and the entrance of reclaimable catalyst transfer lime, the outlet of reclaimable catalyst outlet pipe 26 and the outlet of reclaimable catalyst transfer lime, the entrance of standpipe 5 and the entrance of regenerated catalyst, the outlet 100 i.e. outlet of regenerated catalyst of regenerated catalyst outlet pipe 10.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 distributor 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 and bed formula fluid bed regenerator 60 can be set up in parallel (as shown in Figure 1) with height or height is set up in parallel (as shown in Figure 2).
See 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 diameter, and 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, 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 lower cylinder 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, the cylindrical shell of the cylindrical shell of bed formula fluidized-bed reactor 50 and bed formula fluid bed regenerator 60, blind flange, stripper 18 and various pipeline, 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 pipeline is all coated with an electric heating element and (schemes slightly; Regenerated catalyst outlet pipe 10 is positioned at pipeline section within reactor top cylindrical shell 11, reclaimable catalyst outlet pipe 26 is positioned at except the pipeline section within revivifier top cylindrical shell 1), an electric heating element can be conventional resistance wire or the tile etc. with resistance wire.Parts such as various valves, atomizing feed nozzle 13, fuel oil preheating stove 16, atomization steam boiler 17, stripping gas stove 21, stripping gas distributor 19, main air distributor 3 that the present invention is used, can use fluid catalystic cracking experimental technique field commonly use.Fuel oil preheating stove 16, atomization steam boiler 17, stripping gas stove 21 generally use electrical heater, and atomizing feed nozzle 13 can use 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 the Chinese patent of 201220592166.3.Shown in Fig. 3, this plug valve is used as regeneration plug valve 8; Reference numeral 81 in Fig. 3 represents valve rod, and 82 represent valve cone, and 83 represent valve body, 84 expression valve stem end, and 85 represent plug valve cavitys, 86 expression opening for feeds, and 87 represent discharge port, and 88 represent loosening airduct, and 89 represent loosening wind, and 90 represent lift gas pipe.Valve stem end 84 is connected with electric operator (figure slightly), and electric operator can be bought.Loosen wind 89 and generally use nitrogen.When plug valve described in above patent is used as plug valve 24 to be generated, if 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 into, regenerated catalyst promote gas 7 (nitrogen) change into reclaimable catalyst promote gas 23 (air), loosen wind 89 change air into by nitrogen and change the vergence direction of plug valve, figure omit.Except the plug valve described in above patent, other plug valve meeting application claims also can use.
Illustrating below in conjunction with Fig. 1 and Fig. 2 uses testing apparatus of the present invention to carry out the process tested.Enter atomizing feed nozzle 13 through raw material oil pipe 14 after stock oil 140 is preheated in fuel oil preheating stove 16, water 150 heated in atomization steam boiler 17, form atomizing steam after enter atomizing feed nozzle 13 through atomizing steam pipe 15.Upwards spray through jet exit 130 after stock oil is atomized steam atomizing, 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 bottom, above-mentioned atomized feed oil carries out catalytic cracking reaction with regenerated catalyst counter current contact.The oil gas generated after reaction upwards flows into the dilute phase section on bed formula fluidized-bed reactor 50 top, the oil gas that gas 7 and the stripping gas in stripper 18 after stripping reclaimable catalyst and stripping go out is promoted together with the regenerated catalyst entering this dilute phase section, filter out after catalyzer through reaction oil gas strainer 34 and enter each reaction oil gas arm, enter oil gas product metering recovery finally by reaction oil gas house steward 28, (figure omits analytical system; The distributed data of ethene, propylene and other products can be obtained) by this system.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.Participate in reaction in dense-phase catalyst reaction bed after, the reclaimable catalyst having tied charcoal flows into stripper 18 downwards.Become stripping gas (wherein water becomes water vapor) after water or nitrogen 200 are heated in stripping gas stove 21, enter stripper 18 through stripping gas pipe 20, stripping gas distributor 19.In stripper 18, stripping gas upwards flows, and carries out stripping to the reclaimable catalyst flowed downward, 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, the plug valve cavity through plug valve 24 to be generated passes into reclaimable catalyst to the bottom of spent riser 25 and promotes gas 23 (being generally air), to promote the reclaimable catalyst in spent riser 25.
The reclaimable catalyst 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 bottom, 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 generated after regenerative response upwards flows into the dilute phase section on bed formula fluid bed regenerator 60 top, gas 23 (also burn during use air and become flue gas) is promoted together with the reclaimable catalyst entering this dilute phase section, filter out after catalyzer through regenerated flue gas strainer 33 and enter each root regeneration flue gas arm, enter flue gas cooling finally by regenerated flue gas house steward 27 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, flowed out by the bottom of bed formula fluid bed regenerator 60, enter the top of 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, again participate in catalytic cracking reaction.In said process, the plug valve cavity through regenerating plug valve 8 passes into regenerated catalyst to the bottom of regenerated catalyst riser tube 9 and promotes 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 DEG C, 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 200 ~ 300 millimeters of places above jet exit 130 are measured, and reaction pressure is measured at the top (i.e. the 3rd pressure tap 40 place) of bed formula fluidized-bed reactor 50; Agent-oil ratio is the weight rate (kg/hr) that enters the regenerated catalyst in bed formula fluidized-bed reactor 50 by the outlet 100 of regenerated catalyst outlet pipe 10 and the ratio of weight rate (kg/hr) being entered the atomized feed oil in bed formula fluidized-bed reactor 50 by the jet exit 130 of atomizing feed nozzle 13; (final unit is hour weight space velocity
-1), refer to and enter into the flow (kg/hr) of the atomized feed oil in bed formula fluidized-bed reactor 50 and the ratio of the catalyst inventory (kilogram) in bed formula fluidized-bed reactor 50 by the jet exit 130 of atomizing feed nozzle 13.
In stripper 18, stripping temperature is 400 ~ 550 DEG C; The middle part of this temperature reclaimable catalyst bed height in stripper 18 is measured.In bed formula fluid bed regenerator 60, regeneration temperature is 600 ~ 800 DEG C, 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 DEG C.
Catalyzer can be the catalytic cracking catalyst (catalytic cracking catalyst of the trade mark such as such as MMC-2, CIP-1, RAG-7) of various voluminous low-carbon (LC) gaseous olefin.Before test, first the catalyzer 35 of test is joined in bed formula fluid bed regenerator 60 through catalyst addition tube 30 and catalyzer charging valve 29.Sampling analysis can be carried out to reclaimable catalyst and regenerated catalyst respectively, to determine its carbon content through reclaimable catalyst sampling valve 31 and regenerated catalyst sampling valve 32.
In process of the test, measure the pressure reduction between the first pressure tap 38 and the second pressure tap 39 with differential pressure transmitter, regulate according to this pressure reduction and the difference of setting pressure reduction the aperture regenerating plug valve 8, can catalyst recirculation amount effectively in Control experiment device.The pressure reduction between the 3rd pressure tap 40 and the 4th pressure tap 41 is measured with differential pressure transmitter, the aperture of plug valve 24 to be generated is regulated according to this pressure reduction and the difference of setting pressure reduction, effectively can control the height at dense-phase catalyst reaction bed interface 37 in bed formula fluidized-bed reactor 50, fully ensure the catalytic cracking reaction effect in dense-phase catalyst reaction bed.Above-mentioned measurement, regulate process can complete under control of the computer automatically, and detailed description is omitted.
Use testing apparatus of the present invention, the investigation of the cracking performance of various stock oil and products thereof character, the evaluation etc. of catalyzer can be carried out, meet multiple test objective requirement; Those skilled in the art can design various test subject as required.
Such as, when evaluating a certain catalytic cracking catalyst, a kind of stock oil is first selected to test.Change the principal reaction conditions such as catalytic cracking reaction temperature, reaction pressure, agent-oil ratio, weight space velocity and stock oil oil inlet quantity respectively, research experiment, obtaining this catalytic cracking catalyst and this stock oil can the optimum reaction condition of voluminous low-carbon (LC) gaseous olefin.Then stock oil is replaced by other different types of stock oil, use the same method research experiment under various reaction conditions, and obtaining this catalytic cracking catalyst and other stock oil can the optimum reaction condition of voluminous low-carbon (LC) gaseous olefin.
For another example, when evaluating the cracking performance of a certain stock oil, a kind of catalytic cracking catalyst of first-selected selection is tested.Change the principal reaction conditions such as catalytic cracking reaction temperature, reaction pressure, agent-oil ratio, weight space velocity and stock oil oil inlet quantity respectively, research experiment.Then be other different types of catalytic cracking catalyst by catalyst change, use the same method research experiment under various reaction conditions.Finally by the contrast of each test-results, obtain a kind of be applicable to this kind of stock oil can the optimum catalyst of voluminous low-carbon (LC) gaseous olefin 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), stripping gas distributor (19) is provided with in stripper (18), 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 composition be positioned between the two, 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 on 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 lower cylinder (2) and the inverted round table face shape cylindrical shell composition be positioned between the two, the bottom of revivifier lower cylinder (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 lower cylinder (2) by an inverted round table face shape cylindrical shell, the top on 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 pressed from stripper (18) to the direction of bed formula fluid bed regenerator (60), successively by inclined tube to be generated (22), spent riser (25) and reclaimable catalyst outlet pipe (26) composition, 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 pressed from bed formula fluid bed regenerator (60) to the direction of 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 regenerating 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 distributor (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. the testing apparatus according to claim 3 or 4, is characterized in that: bed formula fluidized-bed reactor (50) and bed formula fluid bed regenerator (60) are set up in parallel with height 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 on 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 on 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 lower cylinder (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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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20100326888A1 (en) * | 2009-06-25 | 2010-12-30 | China Petroleum & Chemical Corporation | Catalytic cracking catalyst having a higher selectivity, processing method and use thereof |
| CN201997317U (en) * | 2011-02-22 | 2011-10-05 | 中国石油天然气股份有限公司 | Reaction regenerating 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20100326888A1 (en) * | 2009-06-25 | 2010-12-30 | China Petroleum & Chemical Corporation | Catalytic cracking catalyst having a higher selectivity, processing method and use thereof |
| CN201997317U (en) * | 2011-02-22 | 2011-10-05 | 中国石油天然气股份有限公司 | Reaction regenerating 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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