CN101029250A - Method and apparatus for producing low-carbon olefine by catalyzing and cracking light-hydrocarbon material - Google Patents
Method and apparatus for producing low-carbon olefine by catalyzing and cracking light-hydrocarbon material Download PDFInfo
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- CN101029250A CN101029250A CN 200710065307 CN200710065307A CN101029250A CN 101029250 A CN101029250 A CN 101029250A CN 200710065307 CN200710065307 CN 200710065307 CN 200710065307 A CN200710065307 A CN 200710065307A CN 101029250 A CN101029250 A CN 101029250A
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Abstract
A method for producing low-carbon olefin is carried out by taking light hydrocarbon as raw material, contacting while pyrolytic reacting light hydrocarbon with pyrolytic catalyst, moving resultant out of reactor while moving inactivated out of moving bed to regenerator for regenerating, and returning it to reactor. It has low reactive temperature, less consumption, high selectivity and better stability.
Description
Technical field
The present invention relates to the catalytic conversion process of petroleum hydrocarbon, specifically, is about a kind of light hydrocarbons to be changed into the method and the production equipment of low-carbon alkenes such as being rich in ethene, propylene, belongs to the petrochemical technology field.
Background technology
Enter after the nineties in 20th century, along with the fast development of petrochemical complex, the domestic and international market increases rapidly the demand of low-carbon alkene such as ethene, propylene.At present, 75% petrochemicals are arranged in the world approximately by ethylene production, ethylene yield has become the sign of weighing a national petrochemical complex industrial development level.China produced 755.53 ten thousand tons of ethene altogether in 2005, increased by 20.43% than 2004.But,, propylene growth of requirement speed has been surpassed rate of growth to ethylene requirements in recent years along with the increasing rapidly of derivatives such as polypropylene.World's Chemical market reached 5,200 ten thousand tons in 2000 to the demand of propylene, expected 2010 and can reach 8,400 ten thousand tons, and average annual rate of growth reaches 6.2%, and the propylene imbalance between supply and demand is also very outstanding.
At present, the method for producing the low-carbon alkene comprise ethene and propylene mainly is steam cracking and catalytic cracking, and wherein steam cracking is to be that raw material is produced ethene and propylene by heat scission reaction with light hydrocarbons such as petroleum naphthas; Catalytic cracking mainly is to be lightweight tank oils such as raw material production gasoline, diesel oil with mink cell focuses such as vacuum gas oils, and low-carbon alkene is the byproduct of this technology.
Increased low carbon olefine output has become the active demand of petroleum chemical industry, if rely on traditional steam cracking to produce the production route of ethene, propylene, will face the restriction of insufficient raw material, poor selectivity; And the temperature of reaction of steam cracking is up to 850 ℃, and production energy consumption is big, running cost is high.For improving the output of low-carbon alkene, each oil refining enterprise is widened raw material sources one after another, and carries out the research that hydrocarbon catalytic cracking is produced low-carbon alkene.Producing low-carbon alkene by catalytic pyrolysis technology has been taken into account the advantage of steam cracking and two kinds of maturation process of catalytic cracking, use high reactivity and high-selectivity catalyst effectively to improve the yield of propylene, reduce the productive rate of low value-added by products such as methane, improved utilization ratio of raw materials; And temperature of reaction reduces about 200 ℃ than steam heat cracking, has significantly reduced production energy consumption.In addition, by changing the Deep Catalytic Cracking process condition, modulation catalytic cracking reaction product distributes flexibly.
In recent years, the Technology that has occurred many cover producing low-carbon alkene by catalytic pyrolysis both at home and abroad.For example, Sinopec petroleum science research institute has developed DCC, ARGG, CPP, MGG mink cell focus producing low-carbon alkene by catalytic pyrolysis technology on riser reactor catalytic cracking process basis, and the ethene of these technologies adds propene yield and reaches about 30%.
The Toyo company of Japan has developed THR technology, and this technology is to be raw material with petroleum naphtha, kerosene, diesel oil and vacuum gas oil, with Ca
12Al
14O
33Be the catalyzer main component, in tubular fixed-bed reactor, lightweight oils such as petroleum naphtha, kerosene and diesel oil carried out catalytic pyrolysis, in fluidized-bed reactor, mink cell focuses such as vacuum gas oil are carried out catalytic pyrolysis.This technology utilizes under less than the 0.1MPa condition high temperature, short contacting time to promote reaction deeply to carry out in 750～850 ℃ of temperature of reaction, reaction pressure, the yield of ethene that this technology obtains is 39.9%, propene yield is 12.4%, byproduct methane yield be 18.6% (1, " technical progress of producing olefin hydrocarbon by catalytic pyrolysis ". Li Xiaoming, Song Furong. petrochemical complex, 2002,31 (7): 569～573; 2, ethene engineering. Chen Bin, Beijing: Chemical Industry Press, 1997).
Russia national organic synthesis institute has developed the Vniios Deep Catalytic Cracking process, this process feeds comprises propane, butane, petroleum naphtha, diesel oil light hydrocarbons raw material and residual oil, employing is potassium vanadate (or vanadic acid sodium) catalyzer of carrier with pottery (andaluzite-corundum), under 780～820 ℃ of conditions of temperature of reaction, react, the reacting middle catalyst coking rate is lower, product yield is an ethene 38.0%, propylene 14.5%, byproduct methane yield is 14.0% (1, Catalytic Pyrolysis of Naphtha on theKVO3-Based Catalyst.Jeong S.M., Chae J.H., Kang J.H., et al, Catalysis Today, 2002,74:257～264; 2, " hydrocarbon catalytic cracking system ethene ". clear spring once, petrochemical complex, 1994,23 (2): 114～120).
Japan company of Asahi Chemical Industry has developed Asahi technology, adopt ZSM-5 and ZSM-11 Si-Al zeolite catalyzer, with the light hydrocarbons petroleum naphtha is that raw material carries out catalytic pyrolysis, the temperature out of reactor is 680 ℃, reaction pressure is 0.1～0.3MPa, the yield of ethene that this technology obtains is 21.8%, propene yield is 22.4%, byproduct methane yield be 12.3% (" external production of propylene technology latest developments and Technological Economy are relatively ". Zhu Minghui, Wang Hongqiu, international petroleum economy, 2006,1:38～42).
The LG company of Korea S has developed a kind of fixed-bed catalytic cracking technology, and this process feeds is the light hydrocarbons petroleum naphtha, adopts modified ZSM-5 catalyst, at 650～680 ℃ of temperature of reaction, weight hourly space velocity 10hr
-1, water-oil ratio 2 condition under react, propylene adds yield of ethene and reaches 50%, and can adjust flexibly ethene and propylene in the product ratio (1, LG Develops Catalytic Naphtha Cracking Process.ChemWeek 2002,164 (21): 24; 2, " hydrocarbon cracking technique for producing ethylene progress ". Sun new people, Liu Lifu, Liu Quanfu, Liaoning chemical industry, 2006,35 (12): 732～735).
The Superflex technology that Germany KBR company has is a kind of fluid catalytic cracking technology, this raw materials technology is light hydrocarbons such as C4, C5 and gasoline fraction, use modified ZSM-5 catalyst, yield of ethene is 20.0% under 560～660 ℃ of conditions of temperature of reaction, and propene yield reaches 40.0%.But this processing requirement raw material must carry out pre-refining, and needs outer heat supplied (" propylene enhancing technology and progress thereof ", Qian Baizhang, refining of petroleum and chemical industry, 2001,32 (11): 20-24).
Germany Lurgi company has developed from the Propylur technology of low value olefin production propylene.Now finished pilot scale research in Lurgi company laboratory, this technology adopts and selects shape type ZSM 5 molecular sieve catalyzer, can be with butylene, amylene in the fixed-bed reactor of 550 ℃ of temperature of reaction, change into propylene to the hexene maximum.The light olefin total conversion rate is about 83%, and propene yield is 42%, yield of ethene is 10%, and the butylene yield is 31% (" propylene enhancing technology and progress thereof ", Qian Baizhang, refining of petroleum and chemical industry, 2001,32 (11): 20-24).
In addition, US 4,980,053 also discloses a kind of technology of using solid acid catalyst production low-carbon alkene with different boiling ranges petroleum fractions, residual oil or crude oil in fluidized-bed or moving-burden bed reactor, reacted catalyzer Returning reactor internal recycle behind coke burning regeneration uses, and the productivity of propylene of this method is up to 26.34%; It is the method that raw material adopts ZSM-5 or ZSM-11 molecular sieve catalyst to produce low-carbon alkene with the vacuum gas oil that WO 00/31215A1 discloses a kind of, propene yield about 20%; Sinopec Shanghai Petroleum Chemical Engineering Institute has proposed that application number is 200510028789.2, denomination of invention is " method that is used for fluidized-bed olefin catalytic cracking to produce propylene, ethene ", use adopts olefin feedstock to produce propylene, ethene by ZSM type molecular sieve, rare earth oxide and phosphorous oxides synthetic catalyzer; Dalian Inst of Chemicophysics, Chinese Academy of Sciences has proposed that application number is 200510086320.4, denomination of invention is " method that catalytically cracked gasoline is produced ethene, propylene and aromatic hydrocarbons ", and this application relates to uses modified molecular sieve catalyst, complex metal oxides and basic catalyst to produce ethene, propylene and aromatic hydrocarbons with catalytically cracked gasoline in fixed bed, riser tube and fluidized-bed reactor.
The catalytic cracking reaction of petroleum hydrocarbon is the carbon rejection process of stock oil, comprises that the high hydrogen richness in these low-carbon alkene purpose products of ethene and propylene must be compensated by heavy hydrocarbon (for example slurry oil) and the coke that reaction generates low hydrogen content.In the catalytic cracking reaction process, lighter products can not infinitely increase, because must keep the balance of protium between raw material and the product, so must produce low value products such as a large amount of slurry oils, coke with heavy hydrocarbon (as vacuum gas oil, wax tailings, long residuum, vacuum residuum) for the raw material low-carbon olefines high-output, make the protium in the heavy oil feed be difficult to be utilized effectively.In general, the H/C of raw material is than the high more low-carbon olefines high-output that helps more, and coke yield is lower.Therefore, with light hydrocarbons (C4 hydrocarbon mixture, petroleum naphtha, catalytic gasoline and the coker gasoline etc. that produce as various oil refining apparatus) is that the technology of raw material production low-carbon alkene can more effectively be utilized petroleum resources, and obtains higher low-carbon alkene purpose product.
The catalytic pyrolysis of light hydrocarbons is the strong endothermic reaction under high temperature, normal pressure (or low pressure) condition, the light hydrocarbons molecule carries out the gas-solid heterogeneous catalytic reaction through the catalytic active center effect and produces low-carbon alkenes such as ethene, propylene, butylene in catalyst surface and duct, and holds concurrently simultaneously and produce the aromatic hydrocarbons that is rich in benzene,toluene,xylene.Because catalytic cracking reaction is the carbon rejection process of hydrocarbon molecules, must have sedimentation of coke that catalyzer is lost activity gradually in catalyst surface and the duct inner reaction process, be 50～100 hours so generally be used for the catalyzer one way life cycle of light hydrocarbons catalytic pyrolysis.Therefore, for the catalytic cracking method and the device of light hydrocarbons, key is to resolve the maintenance problem of catalyst activity in the reaction process.
Develop both at home and abroad at present and realize that industrialized light hydrocarbons preparing low-carbon olefin by catalytically cracking technology great majority are to use fixed-bed reactor, by being entered, raw material after the heating carries out preparing low-carbon olefins by cracking reactions in the reactor, owing to exist catalyzer coking and inactivation simultaneously, cause in the reaction process catalyst activity not keep more for a long time, directly have influence on product selectivity.The reaction of fixed-bed reactor and catalyst regeneration will frequently take turns intermittently to carry out in same reactor aborning, and for heat and the requirement of satisfying catalyst regeneration are provided to reaction, need to be provided with heating plant in the reactor.Therefore, use fixed-bed reactor to have the shortcoming of conversion unit complex structure, production poor continuity.
In order to solve the fast problem of catalyzer coking inactivation that exists in the light hydrocarbons preparing low-carbon olefin by catalytically cracking fixed bed reaction technology, also there is report to adopt fluidized-bed reaction technology, be characterized in reacting and regenerating and in two equipment, carry out respectively.But, because feed composition is lighter, it is so fast that the deactivation rate of catalyzer does not resemble heavy oil catalytic cracking process, and catalyst activity generally can maintain 10～100 hours, so this class catalytic cracking catalyst not too is fit to the fluidization process of frequent reaction regeneration again.In addition, fluidized-bed reaction technology is had higher requirement to catalyst design, require catalyzer to possess preferably the physical strength index that particularly resistance to wears, and hydrothermal stability should be good, and life of catalyst shortens, and has also just increased the cost of catalyzer.
Summary of the invention
The technical problem underlying that institute of the present invention desire solves is to provide a kind of catalytic pyrolysis that utilizes light hydrocarbons to prepare the method for low-carbon alkene, the catalyst regenerator of the catalytic cracking reaction device of moving-bed and moving-bed is combined, in serialization production that realizes scission reaction-catalyst regeneration and operation while, reach the stability of catalyst activity in the raising reaction process and the purpose of catalyzer effective regeneration.
The present invention also provides a kind of production equipment that is used to realize the low carbene technology of above-mentioned preparation, catalyst regenerator reasonable combination with the catalytic cracking reaction device and the moving-bed of moving-bed, can satisfy the serialization production requirement, make whole production system simple in structure, the production efficiency height.
The invention provides a kind of method of utilizing catalyzing and cracking light-hydrocarbon material to prepare low-carbon alkene, this method comprises the steps:
The light hydrocarbons raw material is heated to 560～710 ℃;
Catalytic cracking catalyst is promoted to the top or the top of moving-bed catalytic cracking reactor and imports this reactor;
When described catalytic cracking catalyst is conveyed into reactor, light hydrocarbons raw material after the above-mentioned heating and mixture of steam are sent into this reactor, make catalytic cracking catalyst catalysis light hydrocarbons raw material generation scission reaction in the process that moves down, reaction conditions in the controlling reactor is: temperature of reaction is 550～700 ℃, reaction pressure is 0.05～0.5MPa, and weight hourly space velocity is 0.1～100hr
-1, the translational speed of catalytic cracking catalyst in reactor is: 0.05～0.50m/hr, and the weight ratio of water vapour and light hydrocarbons raw material is 0～2.8 when entering reactor;
The resultant of above-mentioned scission reaction is drawn reactor carry out fractionation and rectification process, and the catalytic cracking catalyst that will move to reactor lower part is drawn from catalyst outlet;
Will be from the moving-burden bed reactor bottom or the outlet at bottom catalytic cracking catalyst of the drawing top or the top that are promoted to the movable bed catalyst revivifier enter revivifier;
Make the catalytic cracking catalyst that enters revivifier and regeneration gas contact reacts and realize regeneration activating, regeneration condition is: regeneration temperature is 450～600 ℃, and regeneration pressure is 0.1～1.0MPa;
Catalyzer behind the regeneration activating is drawn from revivifier bottom or outlet at bottom, promotes from moving-burden bed reactor top or top Returning reactor and recycle by pipeline.
The principal feature of moving-bed is: (1) solid particulate is realized the serialization campaign; (2) allow employed catalyst solid particle grain size a wider range; (3) catalyst solid particle and fluidic can in very large range change duration of contact; (4) catalyst solid particle and fluid approach plug flow and flow the reaction efficiency height; (5) the heat utilization efficiency height of counter current contact.
Applicant's result of study shows, the moving-burden bed reactor technology is used for light hydrocarbons (comprising C4 hydrocarbon mixture, petroleum naphtha, catalytic gasoline and coker gasoline etc. that various oil refining apparatus produce) preparing low-carbon olefin by catalytically cracking technology, and it is combined with the operation of moving-bed revivifier, constantly react and inactivation in moving process by control catalyst, shift out reactor in good time and send into the revivifier regenerating reactivating and recycle, guarantee that catalyzer keeps activity stabilized in reaction process, made full use of the activity performance of catalyzer in one way is used simultaneously.So, adopt technology of the present invention, realizing that the light hydrocarbons resource fully is converted into the low-carbon alkene that is rich in propylene, ethene, and holding concurrently and produce when being rich in the aromatic hydrocarbons of toluene and dimethylbenzene, also be beneficial to and realize the continual and steady of catalyst activity in the serialization of producing and the reaction process.
According to the solution of the present invention, the translational speed of catalyzer in reactor is controlled at 0.05～0.50m/hr (meter/hour), cooperate corresponding reaction conditions, catalyzer is contacted with reactant in slowly moving and give full play to its catalytic activity, on the other hand, because the translational speed of catalyzer wants slow many in fluidized-bed reactor in moving-bed, low to the catalyzer index requirement of resistance to wearing, also wide in range a lot of to the selection of catalysts scope than flowing bed reactor.
Light hydrocarbons raw material of the present invention comprises a kind of or its mixture in C4 hydrocarbon mixture, straight-run spirit (petroleum naphtha), catalytic gasoline, coker gasoline and the visbreaking gasoline etc. that all kinds of oil refining apparatus produce.This light hydrocarbons raw material can be full distillation gasoline for above-mentioned more than one gasoline fraction mixture also, for example: the cut about initial boiling point to 220 ℃; Also can be narrow fraction gasoline, for example: 40～145 ℃ cut.
The inventive method is particularly useful for various catalytic cracking catalysts, for example comprises load metal oxide catalyzer, basic oxide catalyzer or molecular sieve catalyst (comprising modified molecular sieve catalyst) etc.
But the moving-burden bed reactor that the present invention adopts can be the realization response raw material move vertically move axially bed bioreactor, but can also be the realization response raw material radially or the moving-burden bed reactor of the radially moving bed reactor of transverse movement or other form; Correspondingly, light hydrocarbons raw material and the way of contact of catalytic cracking catalyst in reactor can adopt reverse-flowly contact, downflow system contact or cross-current type contact.
According to the particular case and the needs of raw material and catalyzer, the heating of light hydrocarbon raw material realizes by one-level heating unit at least.That is, can heat by one-level, also can be secondary or multistage heat treated; For secondary or multistage heating, can or overlap heating unit more and implement parallel connection or serial operation two covers.
The present invention can also adopt one-level or the above moving-burden bed reactor of one-level to realize the catalytic cracking reaction of light hydrocarbons raw material; When adopting the above reactor of one-level, operate by the serial or parallel connection mode between (two covers or overlap) reactor more.
According to the solution of the present invention, after catalytic cracking catalyst is finished catalytic cracking reaction, enter the regeneration of moving-bed revivifier.
The present invention also provides a kind of device that utilizes catalyzing and cracking light-hydrocarbon material to prepare low-carbon alkene, it comprises and is used to finish the moving-burden bed reactor of catalytic cracking reaction and finishes catalytic cracking catalyst regenerated moving-bed revivifier, moving-burden bed reactor bottom or bottom are provided with catalyst return and are connected with the catalyst inlet of moving-bed revivifier, and moving-burden bed reactor top or top are provided with the regenerated catalyst loop and are connected with the catalyst outlet of moving-bed revivifier; Moving-burden bed reactor also is provided with reactant entrance and product outlet, is connected with the heating unit of light hydrocarbon raw material and the fractionating system of reaction product respectively.
Design key of the present invention is moving-burden bed reactor operation and the operation of moving-bed revivifier are organically combined, the moving-burden bed reactor that is specifically related in the enforcement, moving-bed revivifier and light hydrocarbon heating unit etc. are this area conventional equipment, and its concrete principle of work also is known; The catalyzer that uses then for any catalytic cracking catalyst of realizing the catalytic pyrolysis of light hydrocarbon raw material, the especially catalyzer of some high reactivities, highly selective.
The method of light hydrocarbons preparing low-carbon olefin by catalytically cracking provided by the present invention, its advantage is, utilization has the catalyzer of good catalytic pyrolysis function, catalysis light hydrocarbons raw material is realized catalytic cracking reaction in moving-burden bed reactor, guarantee to react to greatest extent making full use of on the basis of catalyst activity, and can realize the serialization of catalytic cracking reaction-catalyst regeneration, finally reach and make full use of light hydrocarbons and generate and be rich in low-carbon alkenes such as propylene, ethene and hold concurrently and produce the purpose that is rich in aromatic hydrocarbons such as toluene, dimethylbenzene; And the reactive system of this method of enforcement provided by the invention is simple in structure, the production efficiency height.
Description of drawings
Fig. 1 is the indicative flowchart of the inventive method.
Fig. 2 is the embodiment of the invention one reactant and the reverse-flow process schematic representation that contacts of catalyzer;
Fig. 3 is the process schematic representation that the embodiment of the invention two reactants contact with the catalyzer downflow system;
Fig. 4 is the process schematic representation that the embodiment of the invention three reactants contact with the catalyzer cross-current type;
Fig. 5 is the process schematic representation that the embodiment of the invention four reactants contact with the catalyzer cross-current type;
Fig. 6 is the process schematic representation that the embodiment of the invention five reactants contact with the catalyzer cross-current type;
Fig. 7 is the process schematic representation that the embodiment of the invention six reactants contact with the catalyzer cross-current type;
Fig. 8 is the process schematic representation that the embodiment of the invention seven reactants contact with the catalyzer cross-current type.
Embodiment
Further specify embodiment of the present invention and characteristics below in conjunction with accompanying drawing.
At first, as shown in Figure 1, be the schema of a concrete scheme of the present invention.As can be known from Fig. 1, the method for light hydrocarbons preparing low-carbon olefin by catalytically cracking provided by the invention can comprise the steps:
Step 100: the light hydrocarbons raw material is heated to 560～710 ℃ by heating unit, this heating unit can be a cover (one-level heating), also can be many covers (multistage heating), for multistage heating, the above heating unit of two covers can adopt in parallel or placed in-line mode is operated; This light hydrocarbons raw material comprises C4 hydrocarbon mixture, straight-run spirit (petroleum naphtha), catalytic gasoline, coker gasoline and the visbreaking gasoline etc. of various oil refining apparatus generations or the mixture of more than one gasoline fraction, gasoline fraction can be full cut, for example: the cut about initial boiling point to 220 ℃; Also can be narrow fraction, for example: 40～145 ℃ cut.
Step 200: top or top that catalytic cracking catalyst is promoted to moving-burden bed reactor enter reactor, in serialization was produced, catalytic cracking catalyst was to realize recycle from being admitted to reactor by lift line behind the movable bed catalyst revivifier regenerating reactivating.
Step 300: with step 200 while, light hydrocarbons raw material after the heating enters moving-burden bed reactor with water vapour and contacts with the catalytic cracking catalyst that slowly moves down and scission reaction takes place, this reaction conditions is: temperature of reaction is 550～700 ℃, reaction pressure is 0.05～0.5MPa, and weight hourly space velocity is 0.1～100hr
-1, the translational speed of catalytic cracking catalyst in reactor is: 0.05～0.50m/hr, water vapour/light hydrocarbons raw material (weight)=0～2.8: 1; Wherein, the translational speed of catalyzer can determine according to the characteristic of concrete catalyzer and the specification of reactor in above-mentioned scope, and catalyzer activity when reactor shifts out is fully utilized substantially, just can implement manipulation of regeneration basically in good time.
Moving-burden bed reactor bottom or bottom are provided with catalyst return (passing through catalyst outlet) and are connected with moving-bed revivifier top or top, moving-burden bed reactor top or top are provided with (regeneration) catalyst return and link to each other with moving-bed revivifier bottom or bottom, and moving-burden bed reactor can be to move axially bed bioreactor, it can be radially moving bed reactor, can also be rectangular cylinder moving-burden bed reactor for example, particularly:
When employing moves axially bed bioreactor, the light hydrocarbons raw material is contacted or counter current contact realizes catalytic pyrolysis by following current with catalytic cracking catalyst.For example, light hydrocarbons raw material and steam mixture are entered from the bottom or the bottom of reactor, and in reactor, carry out reverse-flow the contact and scission reaction takes place with catalyzer in the motion from bottom to top, reacted resultant (oil gas) is drawn from the top or the top of reactor; Perhaps, light hydrocarbons raw material and steam mixture are entered from the top of reactor, and in reactor, contact with downflow system that catalyzer carries out in the motion from the top down and scission reaction takes place, reacted resultant (oil gas) is drawn from the bottom or the bottom of reactor;
Can also adopt radially moving bed reactor, the light hydrocarbons raw material be contacted by cross-flow with catalytic cracking catalyst realize catalytic pyrolysis.This reactor can be round shape, radially outwards be provided with pipe core from longitudinal center line in the reactor, interior annular space tube and outer annular space tube, interior annular space between interior annular space tube and pipe core forms the catalyst channels as the moving-bed of catalyst layer, and communicate with catalyst inlet, outer annular space between outer annular space tube and interior annular space tube is a reactant channel, utilize pipe core to be the product passage, light hydrocarbons raw material and steam mixture are entered from reactant channel, radially carry out cross-current type along reactor and contact and scission reaction takes place, make reacted resultant oil gas enter pipe core and drawn with the catalyzer that in the moving-bed of catalyst layer, moves down; Perhaps, utilize pipe core to be reactant channel, outer annular space tube is the product passage, light hydrocarbons raw material and steam mixture are entered from reactant channel, radially carry out cross-current type along reactor and contact and scission reaction takes place, make reacted resultant oil gas enter outer annular space and drawn with the catalyzer that in the moving-bed of catalyst layer, moves down; Be flowing of realization response thing and resultant, be provided with the sieve aperture that can pass through for reactant and product as the inner/outer tube wall cloth of the interior annular space of moving-bed of catalyst layer; And reactant entrance can be located at the bottom or the bottom of reactor, also can be located at the top or the top of reactor, and correspondingly, the other end of reactor is located in the product outlet;
Except that above-mentioned round shape radially moving bed reactor, can also adopt the moving-burden bed reactor of other constructional feature, the center is provided with the catalyst channels as the moving-bed of catalyst layer, and a side of moving-bed of catalyst layer is provided with reactant channel, opposite side is provided with the product passage, and they communicate with the reactant entrance and the product outlet of reactor setting respectively; The sidewall that catalyst channels and reactant channel and product passage join is provided with the sieve aperture that can supply reactant and product to pass through, light hydrocarbons raw material and mixture of steam are entered from the reactant channel of a side, transverse flow is crossed reactor, and carry out cross-current type with the catalyzer that in the moving-bed of catalyst layer, moves down and contact and scission reaction takes place, reacted resultant oil gas is drawn from the product passage of moving-burden bed reactor opposite side.For ease of processing with implement, this reactor can be that a kind of profile is the moving-burden bed reactor of rectangular cylinder, and its inside is divided into three passages: catalyst channels and be positioned at the reactant channel and the product passage of its both sides, its cross section can be rectangle.
Step 400: the light hydrocarbons raw material is after reaction under the above-mentioned reaction conditions, scission reaction resultant (oil gas) is drawn reactor send into fractionating system, carry out gas delivery, aromatic hydrocarbons extracting and rectifying, obtain aromatic hydrocarbons such as low-carbon alkenes such as propylene, ethene and benzene,toluene,xylene.
Step 500: with step 400 while, from moving-burden bed reactor top or the catalytic cracking catalyst that enters of top and light hydrocarbons raw material on one side contact reacts slowly move down with suitable speed on one side, draw (this moment, activity of such catalysts lost substantially) from the outlet of reactor lower part or bottom.
Step 600: from the moving-burden bed reactor bottom or the bottom catalyst outlet catalytic cracking catalyst of drawing enter this moving-bed revivifier by top or the top that pipeline is promoted to the moving-bed revivifier.
Step 700: from revivifier top or the catalytic cracking catalyst (loss of activity) that enters of top recover active in internal regenerator and regeneration gas contact reacts, and slowly move down and pass through revivifier, the regeneration condition of catalyzer is in the moving-bed revivifier: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
Step 800: the catalyzer behind the regeneration activating is drawn from revivifier bottom or outlet at bottom, enter into the catalyzer lift line Returning reactor that is connected with reactor top or top, thereby realize going round and beginning again of catalyzer " reaction-regeneration " process, circulation is carried out continuously.
Illustrate: claims of the present invention and specification sheets all are interpreted as moving-burden bed reactor to mentioned " moving-burden bed reactor ", " reactor " in the technical scheme statement, and " moving-bed revivifier ", " revivifier " all are interpreted as the moving-bed revivifier.
Embodiment one:
As shown in Figure 2, be the reverse-flow process schematic representation that contacts of reactant and catalyzer.
After being heated to 560～710 ℃ by heating unit 9, light hydrocarbons 1 and water vapour 7 enters from moving axially bed bioreactor 3 bottoms, catalyzer in moving-bed revivifier 2 behind the regeneration activating is promoted to the top of reactor 3 and enters reactor by pipeline 4, control catalyst speed with 0.05～0.50m/hr in reactor 3 moves down, mobile light hydrocarbons 1 and overheated steam 7 are realized counter current contact and are made light hydrocarbons raw material generation catalytic cracking reaction with entering from the bottom and making progress, 550～700 ℃ of control reaction temperature, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1, water vapour/light hydrocarbons raw material (weight)=0～2.8.The oil gas 6 that the reaction back generates is drawn product after-treatment systems such as entering gas delivery, aromatic hydrocarbons extracting and rectifying from the top of reactor 3, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of reactor 3, enter revivifier 2 by pipeline 5 liftings and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
The oil gas 6 that scission reaction generates is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment two:
As shown in Figure 3, the process schematic representation that contacts with the catalyzer downflow system for reactant.
After the manipulation of regeneration of catalytic cracking catalyst in moving-bed revivifier 2, regenerated catalyst is promoted to the top that moves axially bed bioreactor 3 from the bottom of revivifier 2 by pipeline 4, simultaneously, light hydrocarbons raw material 1 and water vapour 7 are heated to by heating unit 9 that the top from reactor 3 enters after 560～710 ℃, light hydrocarbon raw material and catalyzer are contacted in the reactor following current catalytic cracking reaction takes place simultaneously and control catalyst speed with 0.05～0.50m/hr in reactor 3 moves down, 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1Water vapour/light hydrocarbons raw material (weight)=0～2.8, resultant of reaction oil gas 6 is drawn and sends into product after-treatment systems such as gas delivery, aromatic hydrocarbons extracting and rectifying from the bottom of reactor 3, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of reactor 3, enter revivifier 2 by pipeline 5 liftings and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
The oil gas 6 that scission reaction generates is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment three:
As shown in Figure 4, the process schematic representation that contacts with the catalyzer cross-current type for reactant.
Radially moving bed reactor 3 is a round tube type among the figure, from its central axis radially outwards be provided with pipe core 32, interior annular space tube and outside the annular space tube, the interior annular space 33 that forms between interior annular space tube and pipe core is the catalyst channels as catalyst stream movable bed layer, communicate with catalyst inlet, the reactant channel of outer annular space 31 for communicating of the formation between outer annular space tube and interior annular space tube with reactant entrance, pipe core 32 communicates with the product outlet for the product passage, is provided with the sieve aperture 34 that can supply reactant and product to pass through as the inner/outer tube wall cloth of annular space 33 in the moving-bed of catalyst layer.
Light hydrocarbons 1 and water vapour 7 are heated to by heating unit 9 that the reactant entrance that communicates with reactant channel 31 from moving-burden bed reactor 3 bottoms enters reactor 3 after 560～710 ℃, when moving upward, radially flow through catalyst channels 33, catalytic cracking catalyst is promoted to the top of moving-burden bed reactor 3 through moving-bed revivifier 2 regeneration back by pipeline 4 and enters catalyst channels 33 formation moving-bed of catalyst layers in the reactor 3, and move down with the speed of 0.05～0.50m/hr, in the moving process with upwards mobile light hydrocarbons raw material 1 and water vapour 7 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1, carry out the cross-flow contact under water vapour/light hydrocarbons raw material (weight)=0～2.8 condition and scission reaction take place.Product after-treatment systems such as entering gas delivery, aromatic hydrocarbons extracting and rectifying is drawn in the product outlet that the oil gas 6 that the reaction back generates links to each other with pipe core 32 from reactor 3 tops, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of reactor 3, enter moving-bed revivifier 2 by pipeline 5 liftings and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
The oil gas 6 that scission reaction generates is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment four:
As shown in Figure 5, the process schematic representation that contacts with the catalyzer cross-current type for reactant.
The moving-burden bed reactor of this embodiment and embodiment three are basic identical, and difference only is located at reactor head for the light hydrocarbon feed(raw material)inlet that links to each other with reactant channel 31, and reactor bottom all is located in the product outlet that links to each other with pipe core 32.
Light hydrocarbons 1 is heated to the reactant entrance that links to each other with reactant channel 31 from moving-burden bed reactor 3 tops after 560～710 ℃ with water vapour 7 by heating unit 9 and enters reactor 3, when flowing downward, radially flow through catalyst channels 33, catalytic cracking catalyst is promoted to the top of moving-burden bed reactor 3 through moving-bed revivifier 2 regeneration back by pipeline 4 and enters catalyst channels 33 formation moving-bed of catalyst layers in the reactor 3, and move down with the speed of 0.05～0.50m/hr, in the moving process with the light hydrocarbons 1 that flows downward and water vapour 7 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1Carry out cross-flow contact under water vapour/light hydrocarbons raw material (weight)=0～2.8 condition and react, the product outlet that the oil gas 6 that the reaction back generates links to each other with pipe core 32 from reactor 3 bottoms is drawn and is entered gas delivery, product after-treatment systems such as aromatic hydrocarbons extracting and rectifying, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of reactor 3, enter moving-bed revivifier 2 by pipeline 5 liftings and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
The oil gas 6 that scission reaction generates is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment five:
As shown in Figure 6, the synoptic diagram that contacts with the catalyzer cross-current type for reactant.
The moving-burden bed reactor of this embodiment is similar to embodiment three, the product passage of difference for outer annular space 31 being set to communicate with the product outlet, pipe core 32 is set to reactant channel and communicates with reactant entrance, interior annular space 33 still is a catalyst channels, and the inner/outer tube wall cloth of interior annular space 33 is provided with the sieve aperture 34 that can supply reactant and product to pass through.Light hydrocarbons 1 and water vapour 7 are heated to the reactant entrance that communicates with pipe core 32 from moving-burden bed reactor 3 bottoms after 560～710 ℃ by heating unit 9 and enter reactor 3, when moving upward, radially flow through catalyst channels 33, catalytic cracking catalyst is promoted to the top of moving-burden bed reactor 3 through moving-bed revivifier 2 regeneration back by pipeline 4 and enters catalyst channels 33 formation moving-bed of catalyst layers in the reactor 3, and move down with the speed of 0.05～0.50m/hr, in the moving process with upwards mobile light hydrocarbons raw material 1 and water vapour 7 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1, carry out the cross-flow contact under water vapour/light hydrocarbons raw material (weight)=0～2.8 condition and scission reaction take place.Product after-treatment systems such as entering gas delivery, aromatic hydrocarbons extracting and rectifying is drawn in the product outlet that the oil gas 6 that the reaction back generates communicates with product passage 31 from reactor 3 tops, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of reactor 3, enter moving-bed revivifier 2 by pipeline 5 liftings and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
Scission reaction resultant oil gas 6 is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment six:
As shown in Figure 7, the process schematic representation that contacts with the catalyzer cross-current type for reactant.
The moving-burden bed reactor of this embodiment and embodiment five are basic identical, and difference only is located at reactor head for the light hydrocarbon raw material reaction thing inlet that is connected with pipe core 32, and reactor bottom all is located in the product that is connected with product passage 31 outlet.
Light hydrocarbons 1 is heated to the reactant entrance that links to each other with pipe core 32 from moving-burden bed reactor 3 tops after 560～710 ℃ with water vapour 7 by heating unit 9 and enters reactor 3, when moving downward, radially flow through catalyst channels 33, catalytic cracking catalyst is promoted to the top of moving-burden bed reactor 3 through moving-bed revivifier 2 regeneration back by pipeline 4 and enters catalyst channels 33 formation moving-bed of catalyst layers in the reactor 3, and move down with the speed of 0.05～0.50m/hr, in the moving process with downward light hydrocarbons 1 and overheated steam 7 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1Carry out cross-flow contact under water vapour/light hydrocarbons raw material (weight)=0～2.8 condition and react, the outlet that reacted resultant oil gas 6 links to each other with product passage 31 from reactor 3 bottoms is drawn and is entered gas delivery, product after-treatment systems such as aromatic hydrocarbons extracting and rectifying, the catalyzer of reaction back inactivation then shifts out from the catalyst outlet of the bottom of reactor 3, be raised by pipeline 5 and enter moving-bed revivifier 2 and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
Scission reaction resultant oil gas 6 is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
Embodiment seven:
As shown in Figure 8, the process schematic representation that contacts with the catalyzer cross-current type for reactant.
Moving-burden bed reactor 3 is rectangular cylinder (cross section is a rectangle) among the figure, the centre is the moving-bed of catalyst layer (catalyst channels) 33 of square-section, the one side is the reactant channel 31 of square-section, opposite side is the product passage 32 of square-section, and catalyst channels 33 is laid with sieve aperture 34 with the sidewall that reactant channel 31 and product passage 32 join.
After being heated to 560～710 ℃ by heating unit 9, light hydrocarbons raw material 1 and water vapour 7 enters reactor 3 from moving-burden bed reactor 3 lateral reactant channels 31, catalytic cracking catalyst is promoted to the top of moving-burden bed reactor 3 by pipeline 4 after 2 regeneration of moving-bed revivifier, and catalyzer speed with 0.05～0.50m/hr in the rectangular channel (moving-bed of catalyst layer) 33 of reactor 3 is moved down, light hydrocarbons raw material 1 that enters with the side in the moving process and water vapour 7 are 550～700 ℃ of temperature of reaction, reaction pressure 0.05～0.5MPa, weight hourly space velocity 0.1～100hr
-1Carry out the cross-flow contact under the condition and scission reaction takes place, water vapour/light hydrocarbons raw material (weight)=0～2.8.The oil gas 6 that the reaction back generates is drawn product after-treatment systems such as entering gas delivery, aromatic hydrocarbons extracting and rectifying from reactor 3 another side reactant outlets, the catalyzer of reaction back inactivation then shifts out from the bottom catalyst outlet of moving-burden bed reactor 3, be raised by pipeline 5 and enter moving-bed revivifier 2 and contact regeneration with regeneration gas 8, regeneration condition is: regeneration temperature is 450～600 ℃, regeneration pressure is 0.1～1.0MPa, and regeneration gas is 0.1～21.0% oxygen nitrogen mixture body for the oxygen volume content.
The oil gas 6 that scission reaction generates is collected each cut and product after handling through gas delivery, aromatic hydrocarbons extracting and rectifying etc.
The advantage of utilizing catalyzing and cracking light-hydrocarbon material to prepare the method and apparatus of low-carbon alkene provided by the present invention is, can utilize various catalyzer with good catalytic pyrolysis function, the light hydrocarbons raw material is realized catalytic cracking reaction in moving-burden bed reactor, react to greatest extent making full use of on the basis of catalyst activity, finally reach and make full use of light hydrocarbons and generate and be rich in low-carbon alkenes such as propylene, ethene and hold concurrently and produce the purpose that is rich in aromatic hydrocarbons such as toluene, dimethylbenzene.And, adopt the reactive system of this method simple in structure, the production efficiency height.
Experimental example 1
For verifying effect of the present invention, adopt technical process and the system shown in Fig. 2 (embodiment one), use Daqing crude oil straight-run spirit (petroleum naphtha) and load metal oxide catalytic cracking catalyst, implement cracking under the condition that be 1.4 at 650 ℃ of temperature of reaction, reaction pressure 0.1MPa, water vapour/stock oil, the catalyzer translational speed is 0.25m/hr, and compare with the steam cracking product, the result shows, adopt method of the present invention, the total amount of propylene and the following low-carbon alkene of C4 all has been higher than the steam cracking reaction result in the split product, specifically referring to table 1.
The typical product distribution * of table 1 grand celebration petroleum naphtha catalytic pyrolysis, wt%
| Reaction times, | 400 | 550 | 700 | The catalytic pyrolysis average result | The tube furnace steam cracking |
| Methane | 4.2 | 6.1 | 6.6 | 5.6 | ~15.0 |
| Ethene | 23.5 | 25.5 | 27.3 | 25.4 | ~25.0 |
| Propylene | 30.5 | 25.1 | 26.6 | 27.4 | ~15.0 |
| Butylene | 9.4 | 7.6 | 6.7 | 7.9 | ~11.0 |
| Benzene+toluene+dimethylbenzene | 12.7 | 17.8 | 16.6 | 15.7 | ~10.0 |
| Ethene+propylene | 54.0 | 50.6 | 53.9 | 52.8 | ~40.0 |
| Ethene+propylene+butylene | 63.4 | 58.2 | 60.6 | 60.7 | ~55.0 |
| Ethene+propylene+benzene+toluene+dimethylbenzene | 66.7 | 68.4 | 70.5 | 68.5 | ~50.0 |
| Triolefin+benzene+toluene+dimethylbenzene | 76.1 | 76.0 | 77.2 | 76.4 | ~61.0 |
* catalytic cracking reaction temperature: 650 ℃, steam cracking reaction temperature: 840 ℃.
In the last table, triolefin: ethene, propylene and butylene general name.
Experimental example 2
For verifying effect of the present invention, adopt the technical process shown in Fig. 2 (embodiment one), use hybrid C 4 raw material and modified molecular screen catalytic cracking catalyst, be to implement cracking under the condition of 0.35m/hr in 625 ℃ of temperature of reaction, reaction pressure 0.1MPa, catalyzer translational speed, and compare with steam cracking product (800 ℃ of temperature of reaction), the result shows, adopt method of the present invention, in the catalytic pyrolysis product content of ethene, propylene and aromatic hydrocarbons with and total amount all be higher than the steam cracking reaction result, specifically referring to table 2.
The typical product of table 2 hybrid C 4 catalytic pyrolysis distributes, wt%
| Catalyzer |
| 1# | 2# | 3# | The catalytic pyrolysis average result | The tube furnace steam cracking | |
| Methane | 10.6 | 9.3 | 10.8 | 10.2 | ~15.0 |
| Ethene | 31.2 | 29.5 | 31.9 | 30.9 | ~25.0 |
| Propylene | 18.9 | 25.1 | 20.2 | 21.4 | ~15.0 |
| Benzene+toluene+dimethylbenzene | 25.8 | 18.9 | 26.7 | 23.8 | ~10.0 |
| Ethene+propylene | 50.1 | 54.6 | 52.1 | 52.3 | ~40.0 |
| Ethene+propylene+benzene+toluene+dimethylbenzene | 75.9 | 73.5 | 78.8 | 76.1 | ~50.0 |
Adopt the method and apparatus of embodiment 2～7 to carry out above-mentioned experiment, all can obtain similar result.
Need to prove at last, above embodiment only is used to illustrate technical scheme of the present invention and is unrestricted, although the present invention is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not break away from the spirit and scope of technical solution of the present invention.
Claims (12)
1, a kind of method of utilizing catalyzing and cracking light-hydrocarbon material to prepare low-carbon alkene, it is characterized in that: this method comprises the steps:
The light hydrocarbons raw material is heated to 560～710 ℃;
Catalytic cracking catalyst is promoted to the top or the top of moving-burden bed reactor and imports this reactor;
When described catalytic cracking catalyst is conveyed into moving-burden bed reactor, light hydrocarbons raw material after the above-mentioned heating and mixture of steam are sent into this moving-burden bed reactor, make catalytic cracking catalyst catalysis light hydrocarbons raw material generation scission reaction in the process that moves down, reaction conditions in the control moving-burden bed reactor is: temperature of reaction is 550～700 ℃, reaction pressure is 0.05～0.50MPa, and weight hourly space velocity is 0.1～100hr
-1, the translational speed of catalytic cracking catalyst in moving-burden bed reactor is 0.05～0.50m/hr, the weight ratio of water vapour and light hydrocarbons raw material is 0～2.8 when entering reactor;
The resultant of above-mentioned scission reaction is drawn moving-burden bed reactor carry out fractionation and rectification process, and the catalytic cracking catalyst that will move to reactor lower part is drawn from the outlet of reactor lower part or bottom;
Will be from the moving-burden bed reactor bottom or the outlet at bottom catalytic cracking catalyst of the drawing top or the top that are promoted to the moving-bed revivifier enter this revivifier;
Make the catalytic cracking catalyst that enters the moving-bed revivifier and regeneration gas contact reacts and realize regeneration activating, regeneration condition is: regeneration temperature is 450～600 ℃, and regeneration pressure is 0.1～1.0MPa;
Catalyzer behind the regeneration activating is drawn from revivifier bottom or outlet at bottom, promotes from moving-burden bed reactor top or top Returning reactor and recycle continuously by pipeline.
2, method according to claim 1 is characterized in that: described light hydrocarbons raw material comprises a kind of or its mixture in C4 hydrocarbon mixture, straight-run spirit cut, cat naphtha, coker gasoline cut and the visbreaking gasoline cut that oil refining apparatus produces.
3, method according to claim 1 is characterized in that: adopt to move axially bed bioreactor, the light hydrocarbons raw material is contacted or counter current contact realizes scission reaction with steam mixture in reactor with catalytic cracking catalyst by following current.
4, method according to claim 1, it is characterized in that: adopt radially moving bed reactor, radially outwards be provided with pipe core from longitudinal center line in this reactor, interior annular space tube and outer annular space tube, interior annular space between interior annular space tube and pipe core is the moving-bed of catalyst layer, outer annular space between outer annular space tube and interior annular space tube is a reactant channel, utilize pipe core to be the product passage, light hydrocarbons raw material and steam mixture are entered from reactant channel, radially carry out cross-current type along reactor and contact and scission reaction takes place, make reacted resultant enter pipe core and drawn with the catalyzer that in the moving-bed of catalyst layer, moves down; Perhaps, pipe core is a reactant channel, outer annular space is the product passage, light hydrocarbons raw material and steam mixture are entered from reactant channel, radially carry out cross-current type along reactor and contact and scission reaction takes place, make reacted resultant enter outer annular space and drawn with the catalyzer that in the moving-bed of catalyst layer, moves down.
5, method according to claim 1, it is characterized in that: in the moving-burden bed reactor structure of employing, the centre is provided with the moving-bed of catalyst layer, and a side of moving-bed of catalyst layer is provided with reactant channel, opposite side is provided with the product passage, light hydrocarbons raw material and mixture of steam are entered from reactant channel, transverse flow is crossed reactor, and carry out cross-current type with the catalyzer that in the moving-bed of catalyst layer, moves down and contact and scission reaction takes place, reacted resultant is drawn from the product passage.
6, reaction according to claim 1 is characterized in that: by the heating of one-level heating unit realization light hydrocarbons raw material at least; Adopt the above moving-burden bed reactor of one-level or one-level to realize the catalytic cracking reaction of light hydrocarbons raw material, and during the above reactor of employing one-level, operate by the serial or parallel connection mode between the reactor.
7, method according to claim 1 is characterized in that: described catalytic cracking catalyst comprises load metal oxide catalyzer, basic oxide catalyzer or molecular sieve catalyst.
8, utilize catalyzing and cracking light-hydrocarbon material to prepare the device of low-carbon alkene, it is characterized in that: it comprises and is used to finish the moving-burden bed reactor of catalytic cracking reaction and finishes catalytic cracking catalyst regenerated moving-bed revivifier, moving-burden bed reactor bottom or bottom are provided with catalyst return and are connected with the catalyst inlet of moving-bed revivifier, and moving-burden bed reactor top or top are provided with the regenerated catalyst loop and are connected with the catalyst outlet of moving-bed revivifier; Moving-burden bed reactor also is provided with reactant entrance and product outlet, is connected with the heating unit of light hydrocarbons raw material and the fractionating system of resultant of reaction respectively.
9, device according to claim 8 is characterized in that: described moving-burden bed reactor is for moving axially bed bioreactor.
10, device according to claim 8, it is characterized in that: described moving-burden bed reactor is the round shape radially moving bed reactor, from its central axis radially outwards be provided with pipe core, interior annular space tube and outside the annular space tube, interior annular space between interior annular space tube and pipe core forms the catalyst channels as the moving-bed of catalyst layer, and communicates with catalyst inlet; Outer annular space tube communicates with reactant entrance, and the outer annular space formation reactant channel between interior annular space tube, and pipe core is that the product passage communicates with the product outlet; Perhaps, described outer annular space is the product passage and communicates the reactant channel of pipe core for communicating with reactant entrance with product outlet; Be provided with the sieve aperture that can pass through for reactant and product as the inner/outer tube wall cloth of the interior annular space of moving-bed of catalyst layer.
11, device according to claim 8 is characterized in that: the center of described moving-burden bed reactor is provided with the catalyst channels as the moving-bed of catalyst layer, and communicates with catalyst inlet; One side of catalyst channels is provided with reactant channel, and opposite side is provided with the product passage, and they communicate with reactant entrance and product outlet respectively; The sidewall that catalyst channels and reactant channel and product passage join is laid with the sieve aperture that can supply reactant and product to pass through.
12, according to Claim 8 each described device～11, it is characterized in that: it comprises one or more levels moving-burden bed reactor, when comprising the above moving-burden bed reactor of one-level, between each reactor with the winding of serial or parallel connection mode.
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