CN109666505A

CN109666505A - A kind of technique and system of catalytic pyrolysis

Info

Publication number: CN109666505A
Application number: CN201710959982.0A
Authority: CN
Inventors: 沙有鑫; 朱根权; 谢朝钢; 杨超; 成晓洁
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2017-10-16
Filing date: 2017-10-16
Publication date: 2019-04-23
Anticipated expiration: 2037-10-16
Also published as: CN109666505B

Abstract

The present invention relates to a kind of technique of catalytic pyrolysis and systems, the technique includes: a, the top that heavy charge is sent into downer reactor is contacted with the first catalytic cracking catalyst at the top of downer reactor and from top to bottom carries out the first catalytic cracking reaction, obtains the first product and the first reclaimable catalyst；B, the first product of gained in step a and the first spent agent are sent into first fluidized bed reactor and are contacted with the second catalytic cracking catalyst and carries out the second catalytic cracking reaction, obtain the second product and the second reclaimable catalyst, second reclaimable catalyst is sent into regenerator and is regenerated, regenerated catalyst is obtained.Present invention process and system slow down the increase of dry gas yied while can be improved productivity of low carbon olefin hydrocarbon.

Description

A kind of technique and system of catalytic pyrolysis

Technical field

The present invention relates to a kind of technique of catalytic pyrolysis and systems.

Background technique

The small-numerator olefins such as ethylene, propylene and butylene are most basic organic synthesis raw materials.At present small point in world wide The sub- main production technology of alkene is steam cracking process, but the easy coking of high-temperature cracking furnace, so the technique is substantially with light Matter oil is raw material, such as natural gas, naphtha, light diesel can also be using hydrocracking tail oils as raw material.Crude oil in China weight at present Matter, the trend of in poor quality are more obvious, and the yield of light oil such as naphtha are lower, steam cracking process and catalytic reforming process Raw material imbalance between supply and demand is got worse.Since middle 1980s, China Petrochemical Corp.'s petrochemical industry Research institute begins to the research for the catalytic pyrolysis family technology for being engaged in Producing Low Molecular Olefins from Heavy Oil, and successfully has developed Catalytic pyrolysis (DCC, USP4980053 and USP5670037) technology and maximum the production ethylene of maximum production of propylene are urged Change thermal cracking (CPP, USP6210562).So far, this two kinds of technologies are mainly mentioned with single riser reactor or individually Riser reactors combine the structure of reactor of dense-phase fluidized bed, and dry gas and coke yield are also inclined while improving productivity of low carbon olefin hydrocarbon It is high.

In recent years, the technology of heavy oil pyrolysis low-carbon olefines high-output is carried out by biggish concern using multiple reactors, this A little technologies are all that different reactors is selected for different raw materials, including upstriker reactor, down-flow reactor, or even selection Different catalyst guarantees that various raw materials are reacted under the reaction environment for being more suitable for self-characteristic.

Chinese patent CN101074392A is disclosed a kind of cracked using two-stage catalytic and produces propylene and high-quality petrol and diesel oil Method, this method mainly utilize two-stage riser Catalytic processes, using be rich in shape-selective zeolite catalyst, with heavy crude Hydro carbons or various animals and plants oils rich in hydrocarbon are raw material, carry out feeding manner for reaction mass of different nature Optimum organization, the suitable reaction condition of control different material, with reach improve propene yield, take into account light oil yield and quality, The purpose for inhibiting dry gas and coke to generate.It is specific to propose that the charging of first segment riser is virgin heavy feedstock oil, its underpart or It bottom can be into light hydrocarbon feedstock；Second segment riser charging be high olefin content gasoline and recycle oil, can be layered into Material or mixed feeding, its underpart or bottom can be into other light hydrocarbon feedstocks.

Chinese patent CN101045667A proposes a kind of catalysis conversion method for improving productivity of low carbon olefin hydrocarbon, this method hydrocarbon Oily raw material with regenerated catalyst and optional carbon deposited catalyst through contacting, by cracking in raw material nozzles injection down-flow reactor Product and reclaimable catalyst separation, obtain low-carbon alkene after crackate separation, remaining product at least part introduces riser With regenerative agent haptoreaction in reactor, oil gas is separated with reclaimable catalyst.This method by generate low-carbon alkene with to Raw agent separates in time, tries hard to the secondary response for effectively inhibiting low-carbon alkene, improves the yield of low-carbon alkene.But only with downlink Formula reactor and riser reactor are difficult to meet the conversion ratio of heavy oil and light hydrocarbons, also cannot achieve productivity of low carbon olefin hydrocarbon Maximize, and from the examples of the patent, it can be seen that low-carbon alkene with dry gas yied ratio 3 hereinafter, raw material can not obtain To making full use of, low value products are high.

Chinese patent CN101210191A proposes a kind of down-flow reactor and the concatenated catalysis of riser reactor is split Change method.Feedstock oil after preheating enters down-flow reactor and contacts with the high-temperature regenerated catalyst from regenerator, and vaporization is simultaneously Cracking reaction is carried out, the oil gas for exporting out from down-flow reactor enters riser reactor, and the reaction was continued, anti-from riser Device entrance is answered to introduce another burst of regenerated catalyst, the oil gas for exporting out from riser reactor and catalyst enter sedimentation separation Device separation.According to the difference of target product, the catalyst different from down-flow reactor can be used in riser reactor, it can To improve yield of gasoline, improve product quality.But lighter hydrocarbons do not convert further, therefore productivity of low carbon olefin hydrocarbon will not be very high.

Chinese patent CN102690682A proposes a kind of catalyst cracking method for producing propylene, in this method heavy charge with Using y-type zeolite as the first catalyst of active component the haptoreaction in the first riser；Light hydrocarbon is less than with average pore size The shape-selective zeolite of 0.7nm be active component the second catalyst in the second riser reactor haptoreaction.By resulting oil Gas introducing is reacted with the concatenated fluidized-bed reactor of second reactor.The stripper of catalytic cracking unit partition point It is divided into two independent stripping zones, two stripping zones form two with two risers respectively and independent react, strip and the means of livelihood again Line.

Summary of the invention

The object of the present invention is to provide a kind of technique of catalytic pyrolysis and system, the technique and system can be improved low-carbon alkene Slow down the increase of dry gas yied while Auditory steady-state responses.

To achieve the goals above, the present invention provides a kind of technique of catalytic pyrolysis, which includes: a, by heavy charge Be sent into downer reactor top contacted with the first catalytic cracking catalyst at the top of downer reactor and by up to The first catalytic cracking reaction of lower progress, obtains the first product and the first reclaimable catalyst；B, by step a gained the first product and First reclaimable catalyst, which is sent into first fluidized bed reactor to contact with the second catalytic cracking catalyst and carry out the second catalysis, to be split Solution reaction, obtains the second product and the second reclaimable catalyst, and the second reclaimable catalyst is sent into regenerator and is regenerated, is obtained Regenerated catalyst.

Optionally, which further includes step c: lightweight material being sent into the lower part of riser reactor and comes from riser The third catalytic cracking catalyst of reactor bottom contacts and carries out third catalytic cracking reaction from the bottom to top, obtains third product With third reclaimable catalyst.

Optionally, which further includes step d: gained third product and third reclaimable catalyst feeding being set to described Second fluidized bed reactor above riser reactor carries out the 4th catalytic cracking reaction, obtains the 4th product and the 4th to be generated Catalyst.

Optionally, which further includes step e: the 4th reclaimable catalyst being sent into catalyst blending tank and comes from regeneration The downer reactor is sent into as first catalytic cracking catalyst after at least partly regenerated catalyst mixing of device Top；It is sent remainder regenerated catalyst as second catalytic cracking catalyst and third catalytic cracking catalyst respectively Enter in the first fluidized bed reactor and riser reactor.

Optionally, in step e, on the basis of the total weight of regenerated catalyst for leaving regenerator in the unit time, by 10- The regenerated catalyst of 70 weight % is sent into the catalyst blending tank, described in the regenerated catalyst feeding by 30-60 weight % In first fluidized bed reactor, the regenerated catalyst of 0-40 weight % is sent into the riser reactor.

Optionally, technique further include: second product and/or the 4th product are sent into product separator and produced Object separation, obtains dry gas, liquefied gas, gasoline, diesel oil and slurry oil；Using gained gasoline and/or liquefied gas as the lightweight material It is sent into the riser reactor and carries out the third catalytic cracking reaction.

Optionally, technique further include: be sent into second product in the settling section on first fluidized bed reactor top The settling section is sent out after carrying out gas solid separation, the second reclaimable catalyst is sent into the stripping section of first fluidized bed reactor lower part In stripped after be sent into regenerator in.

Optionally, it is 510-690 DEG C, oil ratio 5-20 that the condition of first catalytic cracking reaction, which includes: temperature, instead It is 0.5-8 seconds between seasonable；The condition of second catalytic cracking reaction includes: that temperature is 480-650 DEG C, weight (hourly) space velocity (WHSV) 1-35 Hour^-1, reaction pressure is 0.15-0.35 megapascal；The condition of the third catalytic cracking reaction includes: that temperature is 520-720 DEG C, Oil ratio is 8-26, and the reaction time is 1-10 seconds；The condition of 4th catalytic cracking reaction includes: that temperature is 500-750 DEG C, Weight (hourly) space velocity (WHSV) is 1-20 hours^-1, reaction pressure is 0.15-0.35 megapascal.

Optionally, the regenerated catalyst includes zeolite, inorganic oxide and optional clay；With the weight of regenerated catalyst On the basis of amount, the content of the zeolite is 1-50 weight %, and the content of inorganic oxide is 5-99 weight %, and the content of clay is 0-70 weight %；The zeolite includes that average pore size less than 0.7 nanometer selects type zeolite and y-type zeolite；In terms of butt and with boiling On the basis of stone total weight, select type zeolite of the average pore size less than 0.7 nanometer is 25-90 weight %, and the y-type zeolite is 10-75 weight %, select type zeolite of the average pore size less than 0.7 nanometer is selected from ZSM series zeolite, ZRP zeolite, the boiling of magnesium alkali At least one of stone, chabasie, dachiardite, erionite, A zeolite, epistilbite and laumontite, the y-type zeolite are selected from dilute At least one of native y-type zeolite, rare earth hydrogen y-type zeolite, ultrastable and extremely steady y-type zeolite of rare earth.

Optionally, the heavy charge is selected from decompressed wax oil, normal pressure wax oil, wax tailings, deasphalted oil, furfural treatment It raffinates oil, at least one of liquefied coal coil, tar sand oil, shale oil, Fischer-Tropsch synthesis oil and animal and plant fat；The lightweight material For gasoline and/or C rich in alkene₄Hydro carbons.

The present invention also provides a kind of system of catalytic pyrolysis, which includes downer reactor, first fluidized bed reaction Device and regenerator；The downer reactor is provided with the catalyst inlet positioned at top, superposed heavy charge entrance With the material outlet for being located at bottom, the first fluidized bed reactor is provided with catalyst inlet, material inlet, catalyst outlet And product exit, the regenerator are provided with catalyst inlet and catalyst outlet；The material outlet of the downer reactor It is connected to the material inlet of the first fluidized bed reactor, the catalyst inlet of the regenerator and the first fluidized bed are anti- The catalyst outlet of device is answered to be connected to, the catalyst inlet of the catalyst outlet of the regenerator and the first fluidized bed reactor It is connected to the catalyst inlet of downer reactor.

Optionally, the system also includes riser reactor, the riser reactor is provided with urging positioned at bottom Agent entrance, positioned at the lightweight material entrance of lower part and positioned at the material outlet at top；The catalyst outlet of the regenerator with The catalyst inlet of the riser reactor is connected to.

Optionally, the system also includes second fluidized bed reactor, the second fluidized bed reactor is provided with material Entrance, product exit and catalyst outlet, the second fluidized bed reactor and riser reactor are coaxially disposed up and down and institute Riser reactor is stated to protrude into from the bottom to top in the material inlet of the second fluidized bed reactor and make riser reactor Top material outlet is located in the second fluidized bed reactor.

Optionally, the system also includes catalyst blending tank, the catalyst blending tank is provided with reclaimable catalyst and enters Mouth, regenerated catalyst inlet and catalyst outlet, the regeneration of the catalyst outlet of the regenerator and the catalyst blending tank Catalyst inlet connection, the reclaimable catalyst of the catalyst outlet of the second fluidized bed reactor and the catalyst blending tank Entrance connection, the catalyst outlet of the catalyst blending tank are connected to the catalyst inlet of the downer reactor.

Optionally, the system also includes product separator, the entrance of the product separator with it is described first-class The product exit of fluidized bed reactor is connected to the product exit of second fluidized bed reactor, and the product separator is provided with dry Gas outlet, liquefied gas outlet, fuel dispensing outlet, diesel oil outlet and slurry oil outlet, the product separator liquefied gas outlet and/ Or fuel dispensing outlet is connected to the feed(raw material)inlet of the riser reactor.

Compared with the prior art, the advantages of the present invention are as follows:

The present invention is based on downer reactor, first fluidized bed reactor and optional riser reactors, second The combined reactor that fluidized bed reactor is constituted is equipped with suitable catalyst by the optimization of process program, realizes that different feeds exist Suitable reactor carries out catalytic pyrolysis, effectively improves heavy oil conversion rate, promotes lightweight material to crack again, dramatically increases low-carbon Olefins yield, while slowing down the increase of dry gas yied.

Downer reactor and first fluidized bed reactor is arranged along the direction that reaction mass flows in the present invention.Utilize downlink Pipe reactor can avoid catalyst air-teturning mixed phenomenon in conventional lift pipe reactor to greatest extent, improve catalyst activity.To Fluidized-bed reactor supplements the high temperature regeneration agent from regenerator to (including the reaction of the severity of first fluidized bed reactor Temperature and oil ratio) regulated and controled, strengthen heavy charge be effectively cracked into the first fluidized bed reactor low-carbon alkene and Gasoline olefin ability is separated reaction product with the reclaimable catalyst of carbon deposit by the efficient gas-solid separating device in settling section, While heavy charge can be made effectively to be cracked into propylene and gasoline, inhibit low-carbon alkene especially propylene splitting after generation again Solution reaction.

The present invention will be enriched in the gasoline and/or C of alkene₄Hydro carbons introduces riser reactor, due to riser reaction zone and The series connection of second fluidized bed reaction zone, it is anti-in low catalyst density can be adjusted flexibly lightweight material according to the demand of reactor product The residence time in area and high catalyst density reaction zone is answered, the cracking of lightweight material is effectively controlled.In lightweight material reaction process Catalyzer coke content is fewer, and catalyst performance variation is not obvious, therefore the air-teturning mixed phenomenon during uplink flowing is to lightweight The influence of raw material reaction is not obvious.And this reclaimable catalyst still has higher activity, can be introduced into downer reactor with Heavy charge contacts and heavy charge is promoted to react.

Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.

Detailed description of the invention

The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:

Fig. 1 includes a kind of flow diagram of specific embodiment of present invention process, also includes the one of present system The structural schematic diagram of kind specific embodiment.

Description of symbols

1 catalyst tank, 2 downer reactor, 3 first fluidized bed reactor

The inclined tube to be generated of 4 settling section, 5 stripping section 6

7 regenerator, 8 regenerator sloped tube, 9 regenerator sloped tube

10 riser reactor, 11 catalyst blending tank, 12 second fluidized bed reactor

13 gas-solid separating device 14,15 product separator of inclined tube to be generated

16 regenerator sloped tube, 17 pipeline, 18 pipeline

19 pipeline, 20 pipeline, 21 pipeline

22 pipeline, 23 pipeline, 24 pipeline

25 pipeline, 26 pipeline, 27 pipeline

28 pipeline, 29 pipeline, 30 pipeline

31 pipeline, 32 pipeline, 33 pipeline

Specific embodiment

Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.

As shown in Figure 1, the present invention provides a kind of technique of catalytic pyrolysis, which includes: a, is sent into down heavy charge The top of row pipe reactor 2 contacted with the first catalytic cracking catalyst from the top of downer reactor 2 and from top to bottom into The first catalytic cracking reaction of row, obtains the first product and the first reclaimable catalyst；B, by gained the first product and first in step a Reclaimable catalyst is sent into first fluidized bed reactor 3 to be contacted and to carry out the second catalytic pyrolysis anti-with the second catalytic cracking catalyst It answers, obtains the second product and the second reclaimable catalyst, the second reclaimable catalyst is sent into regenerator 7 and is regenerated, is obtained again Raw catalyst.

In order to further increase productivity of low carbon olefin hydrocarbon, increase the conversion of lightweight material, which further includes can be with step c: Lightweight material is sent into the lower part of riser reactor 10 and the third catalytic pyrolysis from 10 bottom of riser reactor is catalyzed Agent contacts and carries out third catalytic cracking reaction from the bottom to top, obtains third product and third reclaimable catalyst.And the technique Further preferably include step d: gained third product and third reclaimable catalyst feeding are set on the riser reactor 10 The second fluidized bed reactor 12 of side carries out the 4th catalytic cracking reaction, obtains the 4th product and the 4th reclaimable catalyst.Step c It can be adjusted according to the property and the market demand of lightweight material with step d, if the lightweight material market demand is more, be not necessarily to Starting step c and step d.

According to the present invention, reclaimable catalyst is regenerated, this be it is well-known to those skilled in the art, therefore, should Technique can also include: to carry out gas solid separation in the settling section 4 for be sent into second product 3 top of first fluidized bed reactor After send out the settling section 4, will the second reclaimable catalyst be sent into 3 lower part of first fluidized bed reactor stripping section 5 in carry out vapour It is sent into regenerator 7 after mentioning, gained regenerated catalyst is sent into the lower part of the riser reactor 10, the downer reactor 2 and first bed reactor 3.It should be noted that the progress in order to promote catalytic cracking reaction, low-carbon olefines high-output, It is sent into each reactor as the first catalytic cracking catalyst, the second catalytic cracking reaction and third catalytic cracking reaction again Raw catalyst is without overcooled catalyst, i.e. temperature is between 500-900 DEG C, preferably between 600-800 DEG C.

Coke produced by the reclaimable catalyst as obtained by cracking lightweight material is less, which can also include step Rapid e: the 4th reclaimable catalyst is sent into catalyst blending tank 11 and is mixed at least partly regenerated catalyst from regenerator 7 The top of the downer reactor 2 is sent into as first catalytic cracking catalyst afterwards；By remainder regenerated catalyst 3 He of first fluidized bed reactor is respectively fed to as second catalytic cracking catalyst and third catalytic cracking catalyst In riser reactor 10.

According to the difference of raw material, the regenerated catalyst of different weight is sent into the property of can choose first from the regenerator In fluidized-bed reactor, catalyst blending tank and riser reactor, and optimize the condition of reaction, in step e, with the unit time On the basis of the total weight for inside leaving the regenerated catalyst of regenerator, it will be greater than 0 to less than 100 heavy %, preferably by 10-70 weight % Regenerated catalyst be sent into the catalyst blending tank, will be greater than 0 to less than 100 heavy %, preferably again by 30-60 weight % Raw catalyst is sent into the first fluidized bed reactor 3, and 0- % heavy less than 100 preferably urges the regeneration of 0-40 weight % Agent is sent into the riser reactor 10.

The present invention, which successively passes through lightweight material in riser reactor and second fluidized bed reactor, carries out catalytic pyrolysis, Heavy charge is successively passed through to downer reactor and first fluidized bed reactor carries out catalytic pyrolysis, it can not only be to different originals Material carries out catalytic pyrolysis respectively, improves target product selectivity, can also be lower by phosphorus content obtained by lightweight material cracking reaction The 4th reclaimable catalyst be fed again into downer reactor and first fluidized bed reactor is cracked, and/or by regenerative agent It is sent into first fluidized bed reactor to improve catalyst average activity, increases downer reactor and first fluidized bed reactor The conversion ratio of catalytic pyrolysis.

According to the present invention, in order to separate the second product and the 4th product, which can also include: by described Two products and/or the 4th product are sent into product separator 15 and carry out product separation, obtain dry gas, liquefied gas, gasoline, diesel oil and Slurry oil.The product separator 15 be it is well-known to those skilled in the art, can be fractionating column etc..

According to the present invention, in order to convert the light hydrocarbons in catalytic pyrolysis product, the technique can also include: by Gained gasoline and/or liquefied gas are split as the third catalysis is carried out in the lightweight material feeding riser reactor 10 Solution reaction.

According to the present invention, catalytic pyrolysis is technique well-known to those skilled in the art, and invention repeats no more, described first The condition of catalytic cracking reaction may include: that temperature (downer reactor outlet at bottom) is 510-690 DEG C, preferably 520- 650 DEG C, oil ratio 5-20, preferably 7-18, heavy charge feed atomization vapor accounts for heavy charge and aatomized water vapor weight The 2-50 weight % of the sum of amount preferably accounts for 5-15 weight %, and the reaction time is 0.5-8 seconds, and preferably 1.5-4 seconds, it is anti-to introduce riser Answer the ratio between catalyst of device and first fluidized bed reactor for 1:(1-3)；The condition of second catalytic cracking reaction can wrap Include: temperature is 480-650 DEG C, and preferably 500-640 DEG C, weight (hourly) space velocity (WHSV) is 1-35 hours^-1, preferably 2-33 hours^-1, agent oil Than for 6-20, preferably 7-18, reaction pressure (absolute pressure, outlet pressure) is 0.15-0.35 megapascal, preferably 0.2-0.35 Megapascal；The condition of the third catalytic cracking reaction may include: that temperature (riser reactor top exit) is 520-720 DEG C, preferably 530-700 DEG C, oil ratio 8-26, preferably 10-24, heavy charge feed atomization vapor accounts for heavy charge With the 2-50 weight % of the sum of aatomized water vapor weight, 5-15 weight % is preferably accounted for, the reaction time is 1-10 seconds, preferably 2-7 seconds；Institute State the 4th catalytic cracking reaction condition may include: temperature be 500-750 DEG C, preferably 530-730 DEG C, weight (hourly) space velocity (WHSV) 1- 20 hours^-1, preferably 2-18 hours^-1, reaction pressure (absolute pressure, outlet pressure) is 0.15-0.35 megapascal.

According to the present invention, be for the catalyst of catalytic pyrolysis it is well known to those skilled in the art, be with regenerated catalyst , the catalyst in the regenerated catalyst can be one or more of combinations of the catalyst provided by the prior art, can With commercially available or prepare according to existing method.A kind of specific embodiment, regenerated catalyst may include zeolite, inorganic oxide and Optional clay；On the basis of the weight of regenerated catalyst, the content of the zeolite can be 1-50 weight %, inorganic oxide Content can be 5-99 weight %, and the content of clay can be 0-70 weight %.In addition, in order to improve productivity of propylene and increase conversion Rate, the zeolite may include that average pore size less than 0.7 nanometer selects type zeolite and y-type zeolite；It is in terms of butt and total with zeolite On the basis of weight, select type zeolite of the average pore size less than 0.7 nanometer can be 25-90 weight %, preferably 40-60 weight % is measured, the y-type zeolite can be 10-75 weight %, preferably 30-65 weight %.The average pore size selects type less than 0.7 nanometer Zeolite can be for selected from ZSM series zeolite, ZRP zeolite, ferrierite, chabasie, dachiardite, erionite, A zeolite, epistilbite At least one of with laumontite, and one of above-mentioned zeolite for being obtained after the processing of physically and/or chemically method or two Kind or more mixture.ZSM series zeolite can selected from ZSM-5, ZSM-8, ZSM-11, ZSM-12, ZSM-22, ZSM-23, The mixture of one or more of the zeolite of ZSM-35, ZSM-38, ZSM-48 and other similar structures.Related ZSM-5 More detailed description referring to USP3702886, related ZRP more describe in detail referring to USP5232675, CN1211470A, CN1611299A.The y-type zeolite can be for selected from rare earth Y type zeolite (REY), rare earth hydrogen y-type zeolite (REHY), superstable gamma-type At least one of zeolite (USY) and extremely steady y-type zeolite of rare earth (REUSY).The inorganic oxide is as binder, Ke Yiwei Silica (SiO₂) and/or aluminum oxide (Al₂O₃).Selected clay as matrix, i.e. carrier, can for kaolin and/or Halloysite.

According to the present invention, heavy charge is well-known to those skilled in the art, for example, the heavy charge is heavy hydrocarbon Class and/or various animals and plants oils raw materials rich in hydrocarbon, the heavy hydrocarbon can be for selected from petroleum hydrocarbons, mineral One of oil and synthetic oil or more than one mixture.Petroleum hydrocarbon can be decompressed wax oil, reduced crude, decompressed wax oil The hydrocarbon ils of part reduced pressure residual oil or the acquisition of other secondary operation is blended, the hydrocarbon ils such as wax tailings of the secondary operation acquisition take off Coal tar, furfural treatment one or more of are raffinated oil.Mineral oil can be in liquefied coal coil, tar sand oil and shale oil One or more more than mixture.Synthetic oil can pass through the distillate that F-T is synthesized for coal, natural gas or pitch. The various animals and plants oils rich in hydrocarbon can be various animal and plant fats.The heavy charge preferably is selected from decompression Wax oil, normal pressure wax oil, wax tailings, deasphalted oil, furfural treatment is raffinated oil, liquefied coal coil, tar sand oil, shale oil, Fischer-Tropsch close At at least one of oil and animal and plant fat.

According to the present invention, the lightweight material for introducing riser reactor is preferably enriched in the gasoline and/or C of alkene₄Hydrocarbon, institute State the gasoline fraction that the gasoline rich in alkene is selected from the gasoline fraction that this technique generates and/or the production of other devices.Other devices The gasoline fraction of production can be selected from catalytic cracked naphtha, catalytic cracking stable gasoline, coker gasoline, visbreaker gasoil and One of other oil refining or chemical process gasoline fraction produced or more than one mixture, preferentially select this technique certainly The gasoline fraction of production.The olefin(e) centent of the gasoline rich in alkene can be 25-95 weight %, preferably 35-90 weight % is measured, preferably more than 50 weight %.The end point of distillation of the gasoline rich in alkene is no more than 204 DEG C, such as can be boiling range For 35-204 DEG C of full range gasoline fraction, it is also possible to narrow fraction therein, such as gasoline of the end point of distillation no more than 85 DEG C evaporates Divide, preferably gasoline fraction of the boiling range between 40-85 DEG C.The C₄Hydrocarbon refers to C₄Under fraction room temperature as main component, normal pressure Existing low-molecular-weight hydrocarbon in gaseous form, alkane, alkene and the alkynes for being 4 including carbon atom number, can be this work Skill it is self-produced be rich in C₄The gaseous hydrocarbon products of fraction are also possible to caused by other device processes rich in C₄The gaseous hydrocarbon of fraction, The wherein preferably self-produced C of this technique₄Fraction.The C₄In hydrocarbon, the content of alkene is greater than 50 weight %, preferably greater than 60 weight %, Preferably more than 70 weight %.In lightweight material, C₄The weight ratio of hydrocarbon and gasoline can be (0-2): 1, preferably (0- 1.2): 1, more preferable (0-0.8): 1；Introduce the weight of the gasoline and introducing downer reactor rich in alkene of riser reactor The weight ratio of matter raw material can be (0.05-0.30): 1, preferably (0.10-0.20): 1.

According to the present invention, the outlet preferred lower pressure outlet distributor of the riser reactor, pressure drop can be less than Existing distributor, such as arch distributor etc. can be used in 10KPa, the low tension outlet distributor.

According to the present invention, stripping section stripping vapor and the resulting oil gas of reaction, introduce the bottom of second fluidized bed reactor Reactor is discharged after second fluidized bed device in portion, can reduce oil gas partial pressure, shortens oil gas in settling section residence time, volume increase Productivity of propylene.

As shown in Figure 1, the system includes downer reactor 2, first the present invention also provides a kind of system of catalytic pyrolysis Fluidized-bed reactor 3 and regenerator 7；The downer reactor 2 is provided with the catalyst inlet positioned at top, superposed Heavy charge entrance and material outlet positioned at bottom, the first fluidized bed reactor 3 is provided with catalyst inlet, material enters Mouth, catalyst outlet and product exit, the regenerator 7 are provided with catalyst inlet and catalyst outlet；The down pipe is anti- The material outlet of device 2 and the material inlet of the first fluidized bed reactor 3 is answered to be connected to, the catalyst inlet of the regenerator 7 It is connected to the catalyst outlet of the first fluidized bed reactor 3, the catalyst outlet of the regenerator 7 and the first class The catalyst inlet of bed reactor 3 is connected to the catalyst inlet of downer reactor 2.

In order to further increase productivity of low carbon olefin hydrocarbon, increase the conversion of lightweight material, the system can also include being promoted Pipe reactor 10, the riser reactor 10 is provided with the catalyst inlet positioned at bottom, the lightweight material positioned at lower part enters Mouth and the material outlet positioned at top；The catalyst outlet of the regenerator 7 and the catalyst of the riser reactor 10 enter Mouth connection.And the system further preferably includes second fluidized bed reactor 12, the second fluidized bed reactor 12 is provided with Material inlet, product exit and catalyst outlet, the second fluidized bed reactor 12 and about 10 riser reactor are coaxial It is arranged and the riser reactor 10 protrudes into the material inlet of the second fluidized bed reactor 12 from the bottom to top and makes to mention The top material outlet of riser reactors 10 is located in the second fluidized bed reactor 12.Riser reactor 10 and second Fluidized bed reactor 12 can be adjusted according to the property and the market demand of lightweight material, if the lightweight material market demand compared with Height, then without starting.

Coke produced by the reclaimable catalyst as obtained by cracking lightweight material is less, the system can also include Catalyst blending tank 11, the catalyst blending tank 11 are provided with reclaimable catalyst entrance, regenerated catalyst inlet and catalyst Outlet, the catalyst outlet of the regenerator 7 are connected to the regenerated catalyst inlet of the catalyst blending tank 11, and described second The catalyst outlet of fluidized-bed reactor 12 is connected to the reclaimable catalyst entrance of the catalyst blending tank 11, the catalyst The catalyst outlet of blending tank 11 is connected to the catalyst inlet of the downer reactor 2.

According to the present invention, the riser reactor can for selected from equal diameter riser, etc. linear speeds riser and change One of diameter riser or in which two kinds of combination.The second fluidized bed reactor and the reaction of the independent first fluidized bed Device can be each independently selected from fixed fluidized bed, dispersion fluidized bed, bubbling bed, turbulent bed, fast bed, conveying bed and dense bed The combination of one or more of reactor.

According to the present invention, in order to improve productivity of propylene, the liquefied gas outlet of the product separator 15 and/or gasoline go out Mouth can be connected to the feed(raw material)inlet of the riser reactor 10.

In order to facilitate the separation of product and the regeneration of reclaimable catalyst, the first fluidized bed reactor 3 may include bed Layer conversion zone, the stripping section 5 that is set to below bed conversion zone, the settling section 4 being set to above bed conversion zone, the bed Conversion zone, stripping section 5 and settling section 4 can be coaxially disposed and be in fluid communication, and the bed conversion zone can be set described The first class has can be set in the top of the catalyst inlet and material inlet of fluidized-bed reactor 3, the settling section 4 The product exit of bed reactor 3, the catalyst of the first fluidized bed reactor 3 can be set in the lower part of the stripping section 5 Outlet.

According to the present invention, the second product and the second reclaimable catalyst for leaving first fluidized bed reactor enter settling section, After the second reclaimable catalyst that sedimentation separation wherein carries out, the second product introduces subsequent product separator.In product point From in device, the second product is isolated to dry gas, liquefied gas, gasoline, diesel oil and slurry oil.The second fluidized bed reactor A set of product separator can be shared with first fluidized bed reactor, at this point, introducing product separation after two strands of products are mixed Device.Such as shown in Figure 1, the system can also include product separator 15, the entrance of the product separator 15 It can be connected to the product exit of the product exit of the first fluidized bed reactor 3 and second fluidized bed reactor 12, it is described Dry gas outlet, liquefied gas outlet, fuel dispensing outlet, diesel oil outlet and slurry oil outlet has can be set in product separator 15.It is described Product separator can be the prior art, the present invention do not have particular/special requirement.A kind of specific embodiment, second fluidisation Resulting 4th product of bed reactor reaction and the 4th reclaimable catalyst enter gas-solid separating device.Isolated oil gas enters Product separator is separated.Resulting 4th reclaimable catalyst of gas-solid separating device enters catalyst blending tank, and comes from Wind is pressurized after the high temperature regeneration agent mixing of regenerator to be promoted in catalyst tank.

Technique provided by the present invention is further described with reference to the accompanying drawing:

It is mentioned as shown in Figure 1, high-temperature regenerated catalyst introduces respectively through regenerative agent inclined tube 8, regenerator sloped tube 9, regenerator sloped tube 16 Riser reactors 10, catalyst blending tank 11 and first fluidized bed reactor 3.Preheating or the gasoline rich in alkene not preheated evaporate Divide and/or C4 hydro carbons is after pipeline 23 and the aatomized water vapor from pipeline 24 are mixed in a certain ratio, injecting lift tube reaction Device 10 being mixed and being reacted with via regenerator sloped tube 8 and by the high temperature catalyst risen with promotion air lift from pipeline 22, instead The outlet distributor (not marking in figure) of oil gas and the boosted pipe reactor 10 of catalyst mixture is answered to introduce second fluidized bed anti- Area 12 is answered, the separation that gas-solid separating device 13 carries out oil gas and catalyst is finally entered；Separating obtained oil gas passes through pipeline 25 Into subsequent product separator 15, separating obtained reclaimable catalyst enters catalyst blending tank via inclined tube 14 to be generated 11.High temperature regeneration agent into catalyst blending tank 11 is mixed with the reclaimable catalyst from the second bed reactor, and mixing is urged Agent logistics through pipeline 17 by the pressurization wind from pipeline 33 by being promoted in catalyst tank 1.Heavy charge after preheating is through pipe After line 18 and the aatomized water vapor from pipeline 19 are mixed in a certain ratio, injection downer reactor 2 connects with high temperature intermixture It touches and reacts, outlet distributor (not marking in figure) through downer reactor 2 of reaction oil gas and catalyst mixture introduces the Fluidized-bed reactor 3, the reaction was continued after mixing with the high temperature regeneration agent flowed into via regenerator sloped tube 16, finally enters settling section 4 carry out the separation of oil gas and catalyst；Separating obtained oil gas enters subsequent product separator 15 by pipeline 26.It is producing Reaction product isolates gaseous hydrocarbon (being drawn by pipeline 28), gasoline (being drawn by pipeline 29), diesel oil (by pipe in object separator 15 Line 30 is drawn), light cycle oil (being drawn by pipeline 31) and slurry oil (being drawn by pipeline 32).The cracked gaseous hydrocarbons that pipeline 28 is drawn exist Polymerization-grade propylene product and the C 4 fraction rich in alkene can be obtained after successor separation, purification, wherein the C4 rich in alkene evaporates Point can return to reactor is then converted into ethylene and propylene.The gasoline that pipeline 29 is drawn can partly or entirely Returning reacting system turn again Change, gasoline first can also be cut into light, heavy naphtha section, the part or all of Returning reacting system of light petrol converts again, preferably Light petrol is returned into riser reactor conversion；The isolated catalyst of settling section enters bed reaction zone, subsequently into vapour Section 5 is proposed, stripped vapor is injected through pipeline 20, and carbon deposition catalyst counter current contacting, by reaction oil gas entrained by carbon deposited catalyst It is stripped off as much as possible, then introduces settler through first fluidized bed reactor zone 3, drawn together with other oil gas through pipeline 26 Reactor.Catalyst after stripping is sent into 7 coke burning regeneration of regenerator by inclined tube 6 to be generated.Oxygen-containing gas injects again through pipeline 21 Raw device 7, regenerated flue gas are drawn through pipeline 27.Catalyst after regeneration enters through regenerator sloped tube 16, regenerator sloped tube 8, regenerator sloped tube 9 Different reactor cycles use.During above-mentioned specific embodiment, the pipeline 22 of riser pre lift zone is introduced Pre-lift medium can crack dry gas, the preferred vapor of the present invention selected from vapor, C1~C4 hydro carbons or Conventional catalytic.

The following examples will be further described the present invention, but be not intended to limit the present invention.

Feedstock oil used in embodiment and comparative example is identical with catalyst.Raw material A used is a kind of cracking stock, Specific nature is shown in Table 1.Used catalyst is the MMC-2 of Sinopec Shandong catalyst plant production, is less than containing average pore size 0.7 nanometer of shape-selective zeolite and Y type molecular sieve, specific nature are shown in Table 2.

Embodiment 1

Test carries out in medium-sized cat-cracker.The device includes a set of independent reaction-regeneration system: reactor For downer reactor plus fluidized bed combined reactor, promoting bore is 16 millimeters, and length is 3200 millimeters, downlink tube reaction The diameter (internal diameter) of series fluidized bed reactor at device outlet at bottom, fluidized-bed reactor is 64 millimeters, is highly 600 millimeters. Catalyst used is MMC-2 catalyst, carries out cracking to raw material shown in table 1；Oil gas after reaction is separated with catalyst, is urged Agent enters regenerator regeneration after entering stripper stripping, and the catalyst after regeneration divides two-way to leave regenerator, enters stream all the way Fluidized bed reactor improves reaction temperature and oil ratio in fluidized-bed reactor.Another way enters catalyst blending tank, then into Enter the catalyst tank at the top of downer reactor；Oil gas enters product separator.Its operation condition and reaction result It is shown in Table 3 and table 4.

Comparative example 1

Test carries out in medium-sized cat-cracker.The device includes a set of independent reaction-regeneration system: reactor For riser reactor plus fluidized bed combined reactor, promoting bore is 16 millimeters, and length is 3200 millimeters, promotes tube reaction The diameter (internal diameter) of device top exit series fluidized bed reactor, fluidized-bed reactor is 64 millimeters, is highly 600 millimeters.Institute Catalyst is MMC-2 catalyst, carries out cracking to raw material shown in table 1；Oil gas after reaction is separated with catalyst, catalysis Agent enters regenerator regeneration after entering stripper stripping, is then again introduced into riser reactor and is reacted；Carry out self-fluidized type The reaction product of bed reactor enters product separator.Its operation condition and reaction result are shown in Table 3 and table 4.

Embodiment 2

Referring to embodiment 1, the difference is that regenerator is left on three tunnels of catalyst point after regeneration, enter fluidized-bed reaction all the way Device, another way enter catalyst blending tank, and subsequently into the catalyst tank at the top of downer reactor, third road enters riser Reactor.Riser reactor internal diameter is 12 millimeters, and length is 2200 millimeters, and the catalyst used is MMC-2 catalyst, to next From the light petrol rich in alkene of product separator, (boiling range is 30-85 DEG C, and olefin(e) centent is 52 weight %, light petrol weight Account for 15 weight % of heavy charge weight) cracking is carried out, gained oil gas and catalyst mixture carry out in gas-solid separating device Gas solid separation.Separating obtained catalyst enters catalyst blending tank and mixes with high temperature regeneration agent, is then fed into downer reactor The catalyst tank at top.Separating obtained oil gas product and the oil gas product from settler is mixed into product separator. Its operation condition and reaction result are shown in Table 3 and table 4.

Embodiment 3

Referring to embodiment 2, unlike riser reactor exit set up fluidized-bed reactor, reaction gained oil gas and Catalyst mixture carries out gas solid separation in gas-solid separating device.Separating obtained catalyst enters catalyst blending tank and high temperature Regenerative agent mixing, the catalyst tank being then fed at the top of downer reactor.Separating obtained oil gas product with come from settler Oil gas product be mixed into product separator.Its operation condition and reaction result are shown in Table 3 and table 4.

By table 3 and table 4 as it can be seen that compared with riser reactor adds fluidized-bed reactor, downer reactor adds fluidized bed Reactor can slow down catalyst back-mixing etc. in riser reactor and adversely affect, and slow down while improving productivity of low carbon olefin hydrocarbon dry The increased amplitude of gas yield.Regenerative agent introduces to the concatenated fluidized-bed reactor of downer reactor fluidized bed to can be improved anti- The average activity and reaction temperature of catalyst in device are answered, heavy oil conversion rate and productivity of low carbon olefin hydrocarbon are improved.Riser reactor and Lightweight material is contacted with high temperature catalyst in its concatenated fluidized-bed reactor, be ensure that the conversion ratio of lightweight material, is improved The yield of low-carbon alkene.

Table 1

Project	Raw material A
		Density (20 DEG C), gram-centimeter^-3	0.91
Condensation point, DEG C	34
		Four components, weight %
Saturation point	72.6
		Fragrance point	20.9
Colloid	6.3
		Asphalitine	0.2
Element composition, weight %
		Carbon	86.86
Hydrogen	12.62
		Sulphur	0.46
Nitrogen	0.15
		Boiling range/DEG C
Initial boiling point	271
		10 weight %	362
30 weight %	406
		50 weight %	437
70 weight %	466
		90 weight %

Table 2

Catalyst title	MMC-2
		Main active component	USY+ZRP
Chemical property, weight %
		Al₂O₃	52.3
Na₂O	0.072
		RE₂O₃	0.82
Physical property
		Total pore volume, ml/g	0.183
Micro pore volume, ml/g	0.024
		Specific surface, rice²/ gram	143
Zeolite specific surface, rice²/ gram	50
		Matrix specific surface, rice²/ gram	105
Bulk density, grams per milliliter	0.83
		Micro-activity, weight %	67

Table 3 is the operation condition of embodiment 1-3 and comparative example 1

Case No	Embodiment 1	Comparative example 1	Embodiment 2	Embodiment 3
					Down pipe (riser) reactor
Heavy charge	Raw material A	Raw material A	Raw material A	Raw material A
					Catalyst	MMC-1	MMC-1	MMC-1	MMC-1
Reactor outlet temperature, DEG C	570	570	570	570
					Reaction time, second	1.5	1.5	1.5	1.5
Oil ratio	12.5	12.5	12.5	12.5
					First fluidized bed reactor
Weight (hourly) space velocity (WHSV), hour^-1	3	3	3	3
					Reaction temperature, DEG C	580	550	580	580
Settler pressure, megapascal (absolute pressure)	0.21	0.21	0.21	0.21
					Riser reactor
Lightweight material	/	/	Light petrol	Light petrol
					Catalyst	/	/	MMC-1	MMC-1
Outlet temperature of riser, DEG C	/	/	650	650
					Oil ratio	/	/	22	22
Reaction time, second	/	/	2.1	2.1
					Light petrol and heavy charge weight ratio	/	/	0.15∶1	0.15∶1
Second fluidized bed reactor
					Weight (hourly) space velocity (WHSV), hour^-1	/	/	/	6
Reaction temperature, DEG C	/	/	/	630
					Settler pressure, megapascal (absolute pressure)	/	/	/	0.17

Table 4 is the reaction result of embodiment 1-3 and comparative example 1

Claims

1. a kind of technique of catalytic pyrolysis, the technique include:

A, the top that heavy charge is sent into downer reactor (2) and the first catalysis at the top of downer reactor (2) Catalyst for cracking contacts and from top to bottom carries out the first catalytic cracking reaction, obtains the first product and the first reclaimable catalyst；

B, the first product of gained in step a and the first reclaimable catalyst are sent into first fluidized bed reactor (3) and are urged with second Change catalyst for cracking contact and carry out the second catalytic cracking reaction, obtain the second product and the second reclaimable catalyst, by second to Raw catalyst, which is sent into regenerator (7), to be regenerated, and regenerated catalyst is obtained.

2. technique according to claim 1, which further includes step c:

Lightweight material is sent into the lower part of riser reactor (10) and the third from riser reactor (10) bottom is catalyzed Catalyst for cracking contacts and carries out third catalytic cracking reaction from the bottom to top, obtains third product and third reclaimable catalyst.

3. technique according to claim 2, which further includes step d:

Gained third product and third reclaimable catalyst are sent into the second being set to above the riser reactor (10) Fluidized bed reactor (12) carries out the 4th catalytic cracking reaction, obtains the 4th product and the 4th reclaimable catalyst.

4. technique according to claim 3, which further includes step e:

4th reclaimable catalyst is sent into catalyst blending tank (11) and at least partly regenerated catalyst from regenerator (7) The top of the downer reactor (2) is sent into after mixing as first catalytic cracking catalyst；Remainder is regenerated It is anti-that catalyst as second catalytic cracking catalyst and third catalytic cracking catalyst is respectively fed to the first fluidized bed It answers in device (3) and riser reactor (10).

5. technique according to claim 4, in step e, with left in the unit time regenerator regenerated catalyst it is total On the basis of weight, the regenerated catalyst of 10-70 weight % is sent into the catalyst blending tank, again by 30-60 weight % Raw catalyst is sent into the first fluidized bed reactor (3), and the regenerated catalyst of 0-40 weight % is sent into the riser In reactor (10).

6. technique according to claim 4, the technique further include: be sent into second product and/or the 4th product and produce Object separator (15) carries out product separation, obtains dry gas, liquefied gas, gasoline, diesel oil and slurry oil；

It is sent into the riser reactor (10) using gained gasoline and/or liquefied gas as the lightweight material and carries out described the Three catalytic cracking reactions.

7. technique according to claim 4, the technique further include: second product is sent into first fluidized bed reactor (3) settling section (4) are sent out after carrying out gas solid separation in the settling section (4) on top, the second reclaimable catalyst is sent into first It is sent into regenerator (7) after being stripped in the stripping section (5) of fluidized-bed reactor (3) lower part.

8. technique according to claim 4, wherein the condition of first catalytic cracking reaction includes: that temperature is 510- 690 DEG C, oil ratio 5-20, the reaction time is 0.5-8 seconds；

The condition of second catalytic cracking reaction includes: that temperature is 480-650 DEG C, and weight (hourly) space velocity (WHSV) is 1-35 hours^-1, reaction pressure Power is 0.15-0.35 megapascal；

The condition of the third catalytic cracking reaction includes: that temperature is 520-720 DEG C, oil ratio 8-26, reaction time 1- 10 seconds；

The condition of 4th catalytic cracking reaction includes: that temperature is 500-750 DEG C, and weight (hourly) space velocity (WHSV) is 1-20 hours^-1, reaction pressure Power is 0.15-0.35 megapascal.

9. technique according to claim 4, wherein the regenerated catalyst includes zeolite, inorganic oxide and optional Clay；On the basis of the weight of regenerated catalyst, the content of the zeolite is 1-50 weight %, and the content of inorganic oxide is 5- 99 weight %, the content of clay are 0-70 weight %；

The zeolite includes that average pore size less than 0.7 nanometer selects type zeolite and y-type zeolite；In terms of butt and with zeolite total weight On the basis of, select type zeolite of the average pore size less than 0.7 nanometer is 25-90 weight %, and the y-type zeolite is 10-75 weight % is measured, select type zeolite of the average pore size less than 0.7 nanometer is selected from ZSM series zeolite, ZRP zeolite, ferrierite, water chestnut boiling At least one of stone, dachiardite, erionite, A zeolite, epistilbite and laumontite, the y-type zeolite are to boil selected from Y-type rare earth At least one of stone, rare earth hydrogen y-type zeolite, ultrastable and extremely steady y-type zeolite of rare earth.

10. technique according to claim 2, wherein the heavy charge is selected from decompressed wax oil, normal pressure wax oil, coking Wax oil, deasphalted oil, furfural treatment are raffinated oil, in liquefied coal coil, tar sand oil, shale oil, Fischer-Tropsch synthesis oil and animal and plant fat At least one；The lightweight material is gasoline and/or C rich in alkene₄Hydro carbons.

11. a kind of system of catalytic pyrolysis, which includes downer reactor (2), first fluidized bed reactor (3) and regeneration Device (7)；

The downer reactor (2) is provided with the catalyst inlet positioned at top, superposed heavy charge entrance and position Material outlet in bottom, the first fluidized bed reactor (3) are provided with catalyst inlet, material inlet, catalyst outlet And product exit, the regenerator (7) are provided with catalyst inlet and catalyst outlet；

The material outlet of the downer reactor (2) is connected to the material inlet of the first fluidized bed reactor (3), described The catalyst inlet of regenerator (7) is connected to the catalyst outlet of the first fluidized bed reactor (3), the regenerator (7) Catalyst outlet enter with the catalyst inlet of the first fluidized bed reactor (3) and the catalyst of downer reactor (2) Mouth connection.

12. system according to claim 11, wherein the system also includes riser reactor (10), the promotions Pipe reactor (10) is provided with the catalyst inlet positioned at bottom, the lightweight material entrance positioned at lower part and the material positioned at top Outlet；The catalyst outlet of the regenerator (7) is connected to the catalyst inlet of the riser reactor (10).

13. system according to claim 12, wherein described the system also includes second fluidized bed reactor (12) Second fluidized bed reactor (12) is provided with material inlet, product exit and catalyst outlet, the second fluidized bed reactor (12) and riser reactor (10) is coaxially disposed up and down and the riser reactor (10) protrudes into described second from the bottom to top In the material inlet of fluidized-bed reactor (12) and export the top material of riser reactor (10) positioned at the second In fluidized bed reactor (12).

14. system according to claim 13, wherein the system also includes catalyst blending tank (11), the catalysis Agent blending tank (11) is provided with reclaimable catalyst entrance, regenerated catalyst inlet and catalyst outlet, and regenerator (7) are urged Agent outlet is connected to the regenerated catalyst inlet of the catalyst blending tank (11), the second fluidized bed reactor (12) Catalyst outlet is connected to the reclaimable catalyst entrance of the catalyst blending tank (11), and catalyst blending tank (11) are urged Agent outlet is connected to the catalyst inlet of the downer reactor (2).

15. system according to claim 14, wherein the system also includes product separator (15), the products The product exit and second fluidized bed reactor (12) of the entrance of separator (15) and the first fluidized bed reactor (3) Product exit connection, the product separator (15) are provided with dry gas outlet, liquefied gas outlet, fuel dispensing outlet, diesel oil outlet It is exported with slurry oil, the outlet of the liquefied gas of the product separator (15) and/or fuel dispensing outlet and the riser reactor (10) feed(raw material)inlet connection.