CN101323798B - Catalytic conversion method and special apparatus therefor - Google Patents
Catalytic conversion method and special apparatus therefor Download PDFInfo
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- CN101323798B CN101323798B CN2008101408667A CN200810140866A CN101323798B CN 101323798 B CN101323798 B CN 101323798B CN 2008101408667 A CN2008101408667 A CN 2008101408667A CN 200810140866 A CN200810140866 A CN 200810140866A CN 101323798 B CN101323798 B CN 101323798B
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Abstract
The invention discloses a catalytic conversion method which belongs to the technical field of catalytic conversion of petrolic alkanes. The catalytic conversion is carried out in a first reaction system and a second reaction system sequentially; after raw oil enters the first reaction system for catalytic reaction, all or part of the produced fractions enter the second reaction system in gaseous state and/or liquid state for further catalytic reaction; the first reaction system and the second reaction system respectively use a corresponding catalyst according to different reaction raw materials and target products. By using two reaction systems, the method of the invention using pertinence catalysts to carry out selective catalytic conversion of different fractions, overcomes the deficiencies of poor selectivity and low adjuvant content, and diluting the catalyst when adopting single catalyst, can enhance the productivity of chemical raw materials such as low carbon alkene, etc. and enhance the yield of products; the method overcomes the shortcoming of large energy consumption for cooling and preheating and saves investment, thus greatly enhancing the economical efficiency.
Description
(1) technical field
The invention belongs to petroleum hydrocarbon catalytic conversion technique field, particularly a kind of catalysis conversion method and isolated plant thereof.
(2) background technology
Catalyzed conversion is the most important course of processing in the crude oil secondary processing, and catalyzed conversion forms products such as gasoline, diesel oil, LPG liquefied petroleum gas to petroleum hydrocarbon raw material (comprising atmospheric residue, decompression oil expression, decompressed wax oil, wax tailings etc.) in catalytic convention design.
With ethene, propylene is that the low-carbon alkene of representative is the basic raw material of chemical industry, and existing catalytic conversion technique is a by-product low-carbon alkene when producing gasoline, diesel oil, far can not satisfy the demand of current market to Organic Chemicals.Aromatic hydrocarbons is the important Organic Chemicals that output and scale are only second to ethene and propylene; Its verivate is widely used in Chemicals and fine chemicals such as producing chemical fibre, plastics and rubber; Along with the continuous development of petrochemical complex and textile industry, the demand to aromatic hydrocarbons also constantly increases in the world.Utilizing catalysis conversion method and industrial chemicals such as aromatization technology low-carbon olefines high-output and aromatic hydrocarbons is the new direction that solves shortage of resources, low cost prodn Chemicals, has become current important research project and hot issue.
Catalytic gasoline, coker gasoline be secondary response again, can produce Chemicals such as low-carbon alkene or aromatic hydrocarbons, becomes the important means of chemical industry type catalytic cracking process.
For satisfying the demand and the environmental protection requirement of industrial chemicals rapid growth, except that the various novel flexibility catalyzer of continuous development (like Chinese patent CN1043520, U.S. Pat 6,538,169 and US6,566,293), several kinds of thinkings below the many employings of existing technology:
1, make different fractions return raw oil reactor drum freshening again; Maximum production of propylene like the exploitation of ABB LUMMUS company is technological--and-SCC technology makes self-produced petroleum naphtha above main riser reactor charging, carry out selective reprocessing, can make productivity of propylene further improve 2-3%.
2, the utilization subregion is reflected at reactor drum different positions injection different material or cut; Like CN1898362 a kind of method of producing low-carbon alkene and aromatic hydrocarbons is provided; Raw material contacts with catalytic cracking catalyst; Reaction is carried out at two reaction zones at least, removes the external different liquid reaction product from separation column of purpose product and transforms once more from the different positions Returning reactor.
3, outside the raw oil riser tube; Other builds reactor drum and makes different fractions catalyzed conversion once more; Promptly adopt the multiple reactor form, first reactor drum carries out the reaction of conventional raw oil, and a certain or several fractions such as raw gasline get into and build reactor drum in addition and further transform and obtain the purpose product after fractionation; A kind of catalysis conversion method of producing propylene, butylene and gasoline with low olefine content is disclosed like CN1388216; May further comprise the steps: in hydrocarbon ils (remaining liquid) the injecting lift pipe after (1) preheating; Contact with the catalyzer that contains five-ring supersiliceous zeolite and y-type zeolite and react, the finish mixture gets into fluidized-bed through riser tube; (2) gasoline injects fluidized-bed, contacts with catalyzer from riser tube and reacts; (3) separating oil agent composition, reacted catalyzer through stripping, send in the revivifier and regenerate, the catalyzer after the regeneration returns riser tube and recycles.But this method is increased low carbon olefine output but also can produce the high-quality gasoline of low olefin-content not only.CN1258580C discloses a kind of method for modifying and system of catalyzed conversion gasoline deep reducing olefinic hydrocarbon and increasing octane rating; Be in the reaction-regeneration system of catalytic conversion of heavy oil device, to set up a catalytic reforming reactor drum, the catalyzed conversion gasoline fraction is carried out the catalytic reforming reaction.The catalyzed conversion gasoline fraction of institute's upgrading can be the full cut of raw gasline, raw gasline lighting end or raw gasline last running, and these cuts are set up the B-grade condensation system in fractionator overhead and obtained.
4, in order to increase the productive rate of low-carbon alkene, can adopt to add to be fit to small molecule hydrocarbon cracked " cocatalyst ", generally add the 5-8% of heavy oil catalytic reaction dosage, can increase the propylene of 1-1.5%.
More than these fluidized catalytic conversion (FCC) fall alkene technology and exist some common defectives following with raising the output industrial chemicals technology:
1, different material requires different catalyst, and heavy oit pyrolysis needs the macromolecular cleavage ability of catalyzer high, and generally needs larger aperture; C
4, C
5Cracking then need have the catalyzer of selectivity of light olefin, generally needs smaller aperture due; And above-mentioned existing technology is all used identical catalyzer, promptly only uses a kind of catalyzer.Though for increased low carbon olefine output,, small molecules is further transformed, still when auxiliary agent adds in the FCC catalyzer,, must cause the active reduction of cracking catalyst because catalyzer is produced diluting effect can in revivifier, add the auxiliary agent of 5-8%.The auxiliary agent of common every adding 5%; The heavy oit pyrolysis transformation efficiency reduces by 1 percentage point, and the reduction of heavy oil conversion rate is the important factor that has a strong impact on FCC Technological Economy property, simultaneously since with the heavy oit pyrolysis catalyst mix after; The concentration of auxiliary agent is very low, and the improvement of purpose product is restricted.
2, because the reaction heat that second reactive system needs is more, and green coke is generally less, the regeneration heat release of self green coke can not provide the heat of reaction needed, and second reactive system receives the thermal balance question restriction if utilize original technology to set up independently.
3, various freshening methods all be with cut through separation column separate, heat exchange be cooled to liquid after Returning reactor again; Different fractions earlier is liquid through separation column heat exchange cooling, separate the back directly or through suitably again after the preheating (remaining liquid) return former reactor drum or advance another reactor drum and further transform.Process through cooling earlier heats up has again increased equipment and energy consumption input, and the Technology economy is had a greatly reduced quality.
(3) summary of the invention
The object of the present invention is to provide a kind of catalysis conversion method and isolated plant thereof; Can realize the high yield preparation of multiple product, do not influence each other again, and facility investment be low; Less energy consumption, this method can be used for handling petroleum or coker gasoline raw material production industrial chemicals.
The technical scheme that the present invention adopts is following:
A kind of catalysis conversion method; Said catalyzed conversion carries out in first reactive system and second reactive system successively; Raw oil gets into all or part of cut that produces after the catalyzed reaction in first reactive system and gets into second reactive system with gaseous state and/or liquid form and further carry out catalyzed reaction, first reactive system and different respectively the use corresponding catalyst of second reactive system according to reaction raw materials and purpose product.
Raw oil gets into all or part of cut that produces after the catalyzed reaction in first reactive system and gets into second reactive system with gaseous state and/or liquid form and further carry out catalyzed reaction, the shared reactor drum of gaseous component and/or liquid phase component or use a reactor drum separately separately.
Raw oil gets into all or part of cut that produces after the first reactive system catalyzed reaction and isolates after the heavy constituent residue light constituent earlier and directly get into second reactive system with gaseous form and further carry out catalyzed reaction.
Raw oil gets into the heavy constituent of the part or all of liquid state that produces after the catalyzed reaction in first reactive system and returns first reactive system continuation reaction, and its first reactive system is provided with one or more reactor drums.
The feeding part that gets into second reactive system is from coking, hydrogenation, extracting or other CCUs.
Cool and isolate heavy constituent through heat-exchanger rig; Perhaps isolate heavy constituent through fractionating system, said fractionating system through heat exchange at the bottom of the tower or tower at the bottom of heat exchange and stage casing heat exchange bonded mode separating heavy.
With raw oil is raw material, and the first reactive system temperature of reaction is 450 ℃～530 ℃, reaction times 1.0～5.0s, reaction pressure 0.25～0.50Mpa; The second reactive system temperature of reaction is 450 ℃～660 ℃, reaction times 1.0～150s, reaction pressure 0.20MPa～0.5MPa.
The catalysis conversion method isolated plant; Comprise second reactive system that is connected on first reactive system and the flow process thereafter; Said first reactive system and second reactive system include reactor drum and catalyst regeneration system, and the reactor drum of first reactive system, second reactive system is the single or compound reactor that is selected from riser tube, fluidized-bed, fixed bed.
Be connected with heat-exchanger rig between first reactive system and second reactive system.
Be connected with fractionating system between first reactive system and second reactive system, said fractionating system is provided with the device that refluxes and combine with the middle part heat exchange at the bottom of reflux at the bottom of the tower or the tower.
The inventive method is carried out repeatedly catalytic conversion reaction through two reactive systems; Owing in different reactive systems, carry out, can use different catalyst according to concrete feed properties and product requirement, this has just increased selectivity; Improved efficient; As can raw oil be carried out decarburization, demetalization and heavy oil cracking in first reactive system, and be fit to the small molecules catalyst for reaction and in second reactive system, use, further catalyzed conversion is to produce industrial chemicals such as low-carbon alkene and aromatic hydrocarbons.In addition because all or part of cut that from first reactive system, comes out can directly get into second reactive system with gaseous form; Be that second reactive system provides more heat; Minimizing is to the requirement of heat capacity, therefore overcome second reactive system because of the shortage of heat problem that the green coke quantity not sufficient causes, and having changed simultaneously needs after cooling separates earlier the way of preheating Returning reactor again again; Therefore save facility investment greatly, reduced energy consumption.
Further, will get into second reactive system with gaseous form again from remaining ingredient after the first cutting out partial heavy constituent of all or part of cut of first reactive system.Be more convenient for to the adjustment of the second reactive system selection of catalysts and reaction conditions after heavy constituent are separated, help improving the catalyzed reaction effect of other light constituents and the recovery of purpose product.
Specifically can realize the separation to heavy constituent in the following manner: (1) cools and isolates heavy constituent through heat-exchanger rig.Get into heat-exchanger rig after isolating catalyzer from the reaction product of first reactive system, make the reaction product cooling, the heavy constituent that boiling point is high become liquid discharges, and the light constituent that boiling point is lower still keeps gaseous phase, gets into second reactive system and continues reaction.Heat-exchanger rig can also can be arranged to horizontal for vertical.(2) isolate heavy constituent through fractionating column system, said fractionating column system is only established heat exchange at the bottom of the tower, makes heavy constituent liquefaction, at the bottom of tower, extracts heavy constituent out; As can extract corresponding slurry oil and/or recycle stock partial liquefaction out.(3) isolate heavy constituent through fractionating column system, said fractionating column system is provided with heat exchange at the bottom of stage casing heat exchange and the tower, respectively in separation column bottom and the heavy constituent of stage casing extraction part.As can extract corresponding slurry oil and/or recycle stock partial liquefaction out; Or corresponding slurry oil, recycle stock and the extraction of diesel oil partial liquefaction.With upper type all is heavy constituent to be cooled to liquid from oil gas, isolate; The control of the heat through the heat exchanging device, the adjustment of heat at the bottom of fractionating column system stage casing and/or the tower changed get into the second reactive system oil gas composition, temperature and quantity; Simultaneously can take into account the thermally equilibrated needs of system, those skilled in the art can adjust as the case may be.
Concrete technical process is following: raw oil gets into first reactive system; In first reactive system, carry out catalyzed conversion under the effect of catalyzer; Isolate catalyzer through gas-solid separating device then; Reaction oil gas directly gets into second reactive system with gaseous form through pipeline, or isolates the heavy constituent that need not get into the reaction of second reactive system through heat-exchanger rig or fractionating column system, and light constituent gets into second reactive system with gaseous form through pipeline; Light constituent carries out further catalyzed reaction under the effect of the second reactive system catalyst reactor, generate the purpose product, and the entering subsequent technique is handled; The catalyzer of first reactive system and second reactive system is after gas-solid separating device separates, through getting into revivifier regeneration and recycle behind the stripping stage.
The inventive method first reactive system is mainly used in decarburization, demetalization.
The present invention is through using two reactive systems; Use the specific aim catalyzer that different fractions is carried out the selectivity catalyzed conversion; Overcome poor selectivity when adopting single catalyst, auxiliary agent content is low and to the defectives such as diluting effect that catalyzer produces, the productive rate that can improve industrial chemicals such as low-carbon alkene improves product yield simultaneously; Can directly get into second reactor drum because the reaction oil gas of first reactive system is all or part of with gaseous phase; Be that second reactive system provides more heat; Remedy the few shortcoming of the not enough heat capacity of the second reactive system green coke, can solve the shortage of heat problem of second reactive system easily; Overcome and promptly lowered the temperature and the mass energy consumption of pre-heating temperature elevation, saved investment, economy is increased greatly; The raw material of second reactive system can also can install like catalytic unit, coker from first reactive system and other from first reactive system, can be liquid phase feeding, also can be gas-phase feed, has increased the device processing flexibility.
(4) description of drawings
Fig. 1 is embodiment 1 synoptic diagram.
Fig. 2 is embodiment 2 synoptic diagram.
Fig. 3 is embodiment 3 synoptic diagram.
Fig. 4 is embodiment 4 synoptic diagram.
Fig. 5 is embodiment 5 synoptic diagram.
Fig. 6 is embodiment 6 synoptic diagram.
Fig. 7 is embodiment 7 synoptic diagram.
Fig. 8 is embodiment 8 synoptic diagram.
(5) embodiment:
Below with specific embodiment technical scheme of the present invention is described, but protection scope of the present invention is not limited thereto:
Embodiment 1:
The present embodiment method is as shown in Figure 1, is made up of first reactive system and second reactive system two portions; First reactive system comprises first reactor drum 10, settling vessel 15, stripping stage 16 and catalyst regenerator 18; First reactor drum 10 is a riser tube, and regenerated catalyst inlet 13 is established in the bottom, and standpipe 17, guiding valve to be generated 171 are given birth in stripping stage 16 reception, and revivifier 18 connects regeneration standpipe 181, regeneration guiding valve 182; Establish one-level gas-solid separator 151, secondary gas-solid separator 152 in the settling vessel 15; Second reactive system comprises second riser reactor 20, settling vessel 25, stripping stage 26 and revivifier 28; Regenerated catalyst inlet 23 is established in second riser reactor, 20 bottoms, and standpipe 27, guiding valve to be generated 271 are given birth in stripping stage 26 reception, and revivifier 28 connects regeneration standpipe 281, regeneration guiding valve 282; Establish one-level gas-solid separator 251, secondary gas-solid separator 252 in the settling vessel 25.
The first reactive system reaction process is: 180-250 ℃ raw oil 11 is by after the nozzle atomization; Get into first reactor drum 10; And gasified under the lifting that promotes steam 12 and after the catalyst mix from regenerated catalyst inlet 13, upwards flow along riser reactor and carry out catalyzed reaction.Accomplish reaction afterreaction oil gas and catalyzer and get into settling vessel 15 through the first reactive system outlet pipe 14; By two-stage gas solid separation system 151,152 isolated catalyzer through stripping stage 16 strippings; Get into revivifier 18 regeneration by regeneration standpipe 17, guiding valve to be generated 171, recover active; Reaction oil gas 153 directly gets into second riser reactor, 20 pre lift zones with gaseous phase, carries out the catalyzed conversion of second reactive system.
The second reactive system reaction process is: mix with reaction oil gas 153 from first reactive system under the lifting that promotes steam 22 from the catalyzer of regenerated catalyst inlet 23 and carry out catalyzed reaction.Accomplish reaction afterreaction oil gas and catalyzer and get into settling vessel 25, through stripping stage 26 strippings, got into revivifier 28 regeneration, recover active by regeneration standpipe 27, guiding valve to be generated 271 by two-stage gas solid separation system 251,252 isolated catalyzer; Reaction oil gas 253 goes out device and is for further processing.
The first reactive system oil gas radiating and cooling is 10 ℃ in the present embodiment, all advances second reactive system with gaseous form, and second reactive system uses produces light olefins catalyst.
First reactive system is mainly used in decarburization, demetalization, and reaction conditions is: 495 ℃ of temperature of reaction, the reaction times is 1.5s, reaction pressure 0.30MPa (A), 680 ℃ of regeneration temperatures.535 ℃ of the second reactive system temperature of reaction, reaction times 2.5s, reaction pressure 0.25MPa (A), 650 ℃ of regeneration temperatures.
Raw oil character and product distribute and see table 1.
Embodiment 2:
The present embodiment method is as shown in Figure 2, sets up the heat exchange of formula heat-exchanger rig.Vertical heat-exchanger rig 30 is set between two reactive systems; Reaction oil gas 153 from first reactive system gets into heat-exchanger rig 30; 350 ℃ of cooling temperatures; After the heat exchange cooling, boiling point becomes liquid phase 33 discharges greater than 350 ℃ part, and boiling point gets into second riser reactor, 20 pre lift zones less than 350 ℃ partial reaction oil gas 154 with gas phase state.31,32 is heat transferring medium.
First reactive system is mainly used in decarburization, demetalization, and reaction conditions is, 485 ℃ of temperature of reaction, and the reaction times is 1.5s, reaction pressure 0.30MPa (A), 680 ℃ of regeneration temperatures.535 ℃ of the second reactive system temperature of reaction, reaction times 2.5s, reaction pressure 0.25MPa (A), 630 ℃ of regeneration temperatures.Other are with embodiment 1.
Raw oil character and product distribute and see table 1.
Embodiment 3:
The present embodiment method is as shown in Figure 3, establishes horizontal heat-exchanger rig heat exchange.Horizontal heat-exchanger rig 30 is set between two reactive systems; Reaction oil gas 153 from first reactive system gets into heat-exchanger rig 30; 31,32 is heat transferring medium, and 280 ℃ of cooling temperatures are after the heat exchange cooling; Boiling point becomes liquid phase 33 discharges greater than 280 ℃ part, and boiling point is that heat exchange reaction oil gas 154 gets into second riser reactor, 20 pre lift zones with gas phase state less than 280 ℃ part.
600 ℃ of the second reactor reaction temperature, reaction times 2.0s.Other are with embodiment 2.
Raw oil character and product distribute and see table 1.
Embodiment 4:
The present embodiment method is as shown in Figure 4, and the distillation tower have only heat exchange at the bottom of the tower is set.Reaction oil gas 153 is introduced into separation column 50; This tower is only established heat exchange 51 at the bottom of the tower; Isolated boiling point becomes liquid phase greater than 350 ℃ part 53 and discharges from oil gas 153, and other boiling points are drawn from tower top less than 350 ℃ gaseous component 54 and got into second reactive system, and 52 is recycle pump.Other are with embodiment 2.
Raw oil character and product distribute and see table 1.
Embodiment 5:
The present embodiment method is as shown in Figure 5, establishes heat exchange at the bottom of stage casing heat exchange and the tower.Reaction oil gas 153 is introduced into separation column 50; This tower is established heat exchange 51 and one section stage casing heat exchange 55 at the bottom of the tower; Isolated recycle stock, slurry oil 53 and petroleum naphtha, heavy gas oil component 57 dischargers from oil gas; Boiling point is drawn from tower top less than 250 ℃ gaseous component 58 and is got into second reactive system, and 52,56 is recycle pump.
550 ℃ of the second reactive system temperature of reaction, reaction times 2.7s, other are with embodiment 1.
Raw oil character and product distribute and see table 1.
Embodiment 6:
The present embodiment method is as shown in Figure 6, and second reactor drum is a fixed bed.Reaction oil gas 153 is introduced into separation column 50; This tower is established heat exchange 51 and stage casing heat exchange 55 at the bottom of the tower; Isolated recycle stock, slurry oil 53 and heavy gas oil component 57 dischargers from oil gas; Boiling point is drawn from tower top less than 230 ℃ gaseous component 58 get into second reactive system, 52,56 is recycle pump.Second reactor drum is fixed-bed reactor 41,42.The second reactive system reaction process is: gaseous component 58 reacts, regenerates in fixed- bed reactor 41,42 switchings respectively after the heat exchange, and reaction oil gas 43 goes out device and is for further processing.
Second reactive system uses aromatized catalyst.
The second reactive system reaction conditions is: 500 ℃ of temperature of reaction, reaction times 30s, reaction pressure 0.5MPa (A), 500 ℃ of regeneration temperatures.Other are with embodiment 1.
Raw oil character and product distribute and see table 1.
Embodiment 7:
The present embodiment method is as shown in Figure 7, and second reactive system is established liquid phase component charging and two reactor drums of gaseous component charging.If riser reactor 60; With the 20 shared sedimentations of second reactor drum, regeneration section; The second reactive system reaction process is: be mixed into reactor drum 60 from the regenerated catalyst of revivifier 28 at the lifting that promotes steam 62 isolated petroleum naphtha, diesel component 57 down and from separation column 50 and carry out catalyzed conversion; Gaseous component 58 is drawn from separation column 50 tops and is got into 20 reactions of second reactor drum simultaneously; Two bursts of reactant flow are respectively through gas-solid separator 63 and 251,252, and isolated oil gas is merged into 253 and gone out device and be for further processing.Part petroleum naphtha, diesel component 57A extract out as product.
Other are with embodiment 5.
Embodiment 8:
The present embodiment method is as shown in Figure 8, and first reactive system is provided with two reactor drums.First reactive system is established riser reactor 70 in addition; With the 10 shared sedimentations of first reactor drum, regeneration section; The first reactive system reaction process is: be mixed into reactor drum 70 from the regenerated catalyst of revivifier 18 at the lifting that promotes steam 72 isolated recycle stock, slurry oil 53 down and from separation column 50 and carry out catalyzed conversion; Reactant flow merges into 153 in settling vessel 15 outlets with the first reactor reaction oil gas through gas-solid separator 73 isolated oil gas, gets into subsequent disposal.Diesel oil part 57 is extracted out as product, part recycle stock, slurry oil 53A discharger.
Other are with embodiment 5.
Main operational condition of table 1 embodiment 1-6 and product distribute
Claims (3)
1. catalysis conversion method; It is characterized in that; Said catalyzed conversion carries out in first reactive system and second reactive system successively; Raw oil gets into all or part of cut that produces after the first reactive system catalyzed reaction and isolates after the heavy constituent residue light constituent earlier and directly get into second reactive system with gaseous form and further carry out catalyzed reaction, first reactive system and different respectively the use corresponding catalyst of second reactive system according to reaction raw materials and purpose product.
2. catalysis conversion method as claimed in claim 1; It is characterized in that; Raw oil gets into the heavy constituent of the part or all of liquid state that produces after the catalyzed reaction in first reactive system and returns first reactive system continuation reaction, and its first reactive system is provided with one or more reactor drums.
3. according to claim 1 or claim 2 catalysis conversion method is characterized in that, is raw material with raw oil, and the first reactive system temperature of reaction is 450 ℃～530 ℃, reaction times 1.0～5.0s, reaction pressure 0.25～0.50Mpa; The second reactive system temperature of reaction is 450 ℃～660 ℃, reaction times 1.0～150s, reaction pressure 0.20MPa～0.5MPa.
Priority Applications (1)
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| KR101589565B1 (en) | 2007-12-20 | 2016-01-28 | 차이나 페트로리움 앤드 케미컬 코포레이션 | An improved combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
| TWI418619B (en) * | 2008-12-19 | 2013-12-11 | China Petrochemical Technology Co Ltd | A combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils |
| CN102277194B (en) * | 2010-06-13 | 2013-11-06 | 青岛京润石化设计研究院有限公司 | Catalytic conversion method |
| CN102453500A (en) * | 2010-10-21 | 2012-05-16 | 中国石油化工股份有限公司 | Catalytic cracking method and equipment for hydrocarbon oil |
| CN106893609A (en) * | 2015-12-21 | 2017-06-27 | 中国石油天然气集团公司 | Produce the device and method of propylene content cracked gas high and gasoline with low olefine content |
| CN106861562A (en) * | 2017-03-25 | 2017-06-20 | 上海复榆新材料科技有限公司 | A kind of reaction unit for preparing Si hydrophobic Y zeolite adsorbents high |
| CN107286972B (en) * | 2017-07-21 | 2019-11-22 | 石宝珍 | A kind of catalysis conversion method of producing more propylene |
| CN111704927B (en) * | 2020-07-09 | 2022-04-15 | 青岛京润石化设计研究院有限公司 | Method and device for preparing olefin and aromatic hydrocarbon by catalytic conversion of petroleum hydrocarbon raw material |
| CN111718231B (en) * | 2020-07-09 | 2023-07-04 | 青岛京润石化设计研究院有限公司 | Method and device for preparing ethylene and propylene by catalytic conversion of crude oil |
| WO2022048440A1 (en) * | 2020-09-02 | 2022-03-10 | 青岛京润石化设计研究院有限公司 | Method and device for preparing propylene and ethylene by using catalytic conversion of petroleum hydrocarbons |
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| CN1205319C (en) * | 1998-05-05 | 2005-06-08 | 埃克森研究工程公司 | Two stage fluid catalytic cracking process for selectively producing C2-C4 olefins |
| CN101228104A (en) * | 2005-10-07 | 2008-07-23 | Sk能源株式会社 | Method for increasing yield of light olefins in catalytic cracking reaction of hydrocarbon feedstock |
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| CN1205319C (en) * | 1998-05-05 | 2005-06-08 | 埃克森研究工程公司 | Two stage fluid catalytic cracking process for selectively producing C2-C4 olefins |
| CN101228104A (en) * | 2005-10-07 | 2008-07-23 | Sk能源株式会社 | Method for increasing yield of light olefins in catalytic cracking reaction of hydrocarbon feedstock |
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