CN102371167A - Fluidized bed catalyst and its preparation method - Google Patents
Fluidized bed catalyst and its preparation method Download PDFInfo
- Publication number
- CN102371167A CN102371167A CN2010102615445A CN201010261544A CN102371167A CN 102371167 A CN102371167 A CN 102371167A CN 2010102615445 A CN2010102615445 A CN 2010102615445A CN 201010261544 A CN201010261544 A CN 201010261544A CN 102371167 A CN102371167 A CN 102371167A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- roasting
- molecular sieve
- weight
- preparation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention relates to a fluidized bed catalyst and its preparation method, and mainly solves the problems of poor strength and low wear resistance of fluidized bed catalysts in the prior art. The preparation method provided by the invention comprises the following steps of: (a) uniformly dispersing a molecular sieve, a binder, a matrix material, a pore-expanding agent, a dispersant and a liquid medium to form a fluid suspension; (b) carrying out high-speed shearing on the fluid suspension, and controlling the granularity of the materials in the fluid suspension within 0.1-5 microns; (c) adding a wear-resisting agent into the fluid suspension, and uniformly stirring; (d) carrying out spray drying on the fluid suspension to form a microspheric catalyst; (e) roasting the microspheric catalyst to form the finished product catalyst. The technical scheme provided by the invention greatly solves the problems and can be applied in the reaction process of producing light olefin by light oil catalytic cracking.
Description
Technical field
The present invention relates to a kind of fluid catalyst and preparation method thereof, particularly about molecular sieve fluid bed catalyst of a kind of reaction that is used for the naphtha catalytic cracking producing light olefins and preparation method thereof.
Background technology
Ethylene, propylene industry has critical role as the tap of petrochemical industry in the national economic development.Along with the development of society, the market demand of China's ethylene, propylene sharply increases, and the import volume of ethylene, propylene and downstream product thereof increases year by year, and the home products occupation rate of market is less than half the.Ethene and propylene can be used for producing plastics and other chemical products, are important Organic Chemicals, and along with the progress and the development of modern society, its demand is increasing.Ethylene yield more than 98% comes from steam cracking technology in the world at present, and production of propylene mainly produces the joint product of ethene with steam cracking and two kinds of forms of byproduct of oil plant catalytic cracking obtain.
Molecular sieve is applied in field of petrochemical industry widely owing to have good shape selective catalysis performance and heat endurance preferably.When molecular sieve is applied to Industrial Catalysis, generally can not adopt 100% molecular sieve to be prepared into catalyst applications in industrial process.Self caking property of molecular sieve is poor, and self granularity is too tiny, even compression molding, intensity also is lower than 20 newton, is difficult to be shaped to the catalyst that directly applies to industrial process.The manufacturing cost of molecular sieve is generally than higher, if adopt 100% molecular sieve as industrial catalyst, with making the operating cost of industrial process increase.Industrial process generally requires catalyst to possess certain shape and intensity to be adapted to industrial reactor.For fixed bed reactors, catalyst need not to move after installing, but catalyst need possess certain crush strength, and to prevent in dress agent process that catalyst is hit and damaged, and the catalyst that prevents to be installed in lower floor is owing to bearing pressure and breakage.The rising that the damaged efflorescence of catalyst possibly cause device pressure to fall, reflex action may occur unusually, and the product composition changes, and is unfavorable for the goal response process.For fluidized-bed reactor; Because this constantly circulates catalyst in reactor or turbulence; Friction between catalyst granules and particle, catalyst and wall of reactor, catalyst and regenerator wall, catalyst and heat collector wall, catalyst and the conveyance conduit wall and collision all can make catalyst levigate and damaged, final form effusion reaction system with fine powder.These fine powders pollute the environment, and the use cost of catalyst is risen.Therefore, no matter be that molecular sieve is applied to fixed bed reactors, still be applied to fluidized-bed reactor, all need pass through molecular sieve and carrier material the effect formation molecular sieve catalyst composition of binding agent; This combination of molecular sieve can have catalytic activity, selectivity, stability, shape and intensity concurrently simultaneously, thereby satisfies the requirement of industrial process to catalyst.
The US6509290 patent discloses a kind of method for preparing molecular sieve catalyst, contains molecular sieve in this catalyst and grinds particle and initial molecule sieve.This grinds particle mainly from the broken particle of Catalyst Production technology and reaction system recirculation.This method comprises molecular sieve, original binding agent and filler, spray-diredly grinds particle or agglomerate and be mixed together from the non-original particle that grinds of reaction unit.This mixture is dry, form the finished product catalyst granules.In order to increase the intensity of catalyst granules, this grinds particle and is substantially free of coke.
The US6153552 patent research a kind of method for preparing molecular sieve catalyst; This method comprises molecular sieve and alumina sol is mixed together; This alumina sol prepares in solution and remains under 2～10 the pH value, and this mixture of spray-drying and high-temperature roasting makes wear-resistant catalyst.
The CN1791463 patent discloses a kind of method for preparing molecular sieve catalyst, and this method comprises that the molecular sieve catalyst with molecular sieve, liquid and effective big drying of hardening capacity is mixed together the formation slurry, and roasting behind dry this slurry forms wear-resistant catalyst.
Although more existing patents have related to the preparation method of fluid catalyst, the scuff resistance of fluid catalyst is lower, needs further to improve.
Summary of the invention
One of technical problem to be solved by this invention is the relatively poor problem of molecular sieve fluid bed catalyst anti-wear performance that exists in the prior art, and a kind of new fluid catalyst is provided.This catalyst has the advantage that fluid effect is good, scuff resistance is high, catalytic performance is good.
For one of addressing the above problem, the technical scheme that the present invention adopts is following: a kind of fluid catalyst in the finished catalyst weight percentage after the roasting, comprises following material composition:
A.10～60% molecular sieve;
B.2～40% binding agent;
C.10～60% matrix;
D.0.1～30% anti-wear agent;
Wherein, anti-wear agent is for being selected from bar-shaped or the needle inorganic material, and its draw ratio is 2～20.
In the technique scheme; The anti-wear agent preferred version is to be selected from a kind of in asbestos, ceramic fibre, glass fibre, the wollastonite mineral; The draw ratio preferable range of anti-wear agent is 3～10, and in the finished catalyst weight after the roasting, anti-wear agent content preferable range is 1～15%; The molecular sieve preferred version is to be selected from least a in ZSM-5, modenite, β zeolite, Y zeolite, MCM-22, ZSM-5/ modenite, ZSM-5/ β zeolite or the ZSM-5/Y zeolite; The crystal particle diameter preferable range of molecular sieve is between 0.1～5um; The density preferable range of molecular sieve is at 0.5～2 grams per milliliter; In the finished catalyst weight after the roasting, the molecular sieve content preferable range is 10～50%; The binding agent preferred version is to be selected from least a in Ludox or the aluminium colloidal sol, and in the finished catalyst weight after the roasting, the binder content preferable range is 5～20%; The host material preferred version is to be selected from least a in kaolin, calcined kaolin, diatomite, bentonite or the carclazyte, and in the finished catalyst weight after the roasting, the matrix material content preferable range is 15～50%.
Two of technical problem to be solved by this invention provides a kind of preparation method of the new fluid catalyst of one of dealing with problems, and the fluid catalyst of this method preparation has the high advantage of scuff resistance.
For address the above problem two, the technical scheme that the present invention adopts is following: (a) molecular sieve, binding agent, host material, expanding agent, dispersant and liquid medium are evenly disperseed to form suspension, the suspension solids content is 10～50%; (b) adopt in the method control suspension of high speed shear or circulating emulsion raw meal particle size between 0.5～5um; (c) in suspension, add anti-wear agent, stir again; (d) this suspension of spray-drying forms microspherical catalyst; (e) this microspherical catalyst of roasting forms finished catalyst.
In the technique scheme; The expanding agent preferred version is to be selected from least a in methylcellulose, polyvinyl alcohol, sesbania powder, soluble starch or the CNT; In contained molecular sieve weight in the finished catalyst weight after the roasting, the consumption preferable range of expanding agent is 0.1～10%; The dispersant preferred version is to be selected from least a in Triammonium citrate, ammonium oxalate, ammonium carbonate or the carbonic hydroammonium, and in contained molecular sieve weight in the finished catalyst weight after the roasting, the consumption preferable range of dispersant is 0.01～10%; The middle material particular diameter preferable range of method control step (b) that adopts high speed shear or circulating emulsion is between 0.1～2um; (a) step suspension solids content preferable range is 10～50%; The spray shaping condition is 180～300 ℃ of inlet temperatures, 100～160 ℃ of outlet temperatures, and 5000～15000 rev/mins of centrifugal rotational speeds, exit whirlwind pressure reduction is 0.5～1.0KPa, charging rate is 0.5～5 kilogram/hour; The catalyst of spray-drying preparation is through after the high-temperature roasting; The average grain diameter of particle is between 50～90um, and specific area is between 100～300, and average pore size is between 1～20nm; Density between 0.6～1.2 grams per milliliter, abrasion index 0.01～1.2 weight %/hour; Binding agent accounts for 10～40 weight % in the catalyst that makes; Molecular sieve accounts for 10～50 weight %; Matrix material accounts for 10～80 weight %.
In the technical scheme of the present invention,, each component is evenly disperseed through adding at least a dispersant in Triammonium citrate, ammonium oxalate, ammonium carbonate or the carbonic hydroammonium; Be difficult for reuniting; After adopting emulsify at a high speed to shear, suspension is difficult for layering or deposition, and the catalyst surface of preparing is smooth; Sphericity is high; Owing in catalyst preparation process, added at least a expanding agent in methylcellulose, polyvinyl alcohol, sesbania powder, soluble starch or the CNT, the diffusion of catalyst is better again, and is active higher.Because the slurry of preparation evenly, can combine closely between each material, the alternate combination of each thing of the catalyst of preparation is tight, and the finished catalyst that obtains has higher scuff resistance; Because the slurry of preparation is even; Can combine closely through having added the very high crystal anti-wear agent of elongated intensity, having made between each component in the catalyst, each material, the finished catalyst that obtains has higher scuff resistance; Its abrasion index can reach 0.001 weight %/hour, obtained better technical effect.
Through embodiment the present invention is done further elaboration below, but be not limited only to present embodiment.
The specific embodiment
[embodiment 1]
Take by weighing 500 gram kaolin, sesbania powder 2 grams and draw ratio and be 8 wollastonite 20 grams, after mixing, add 2000 gram distilled water; With high-speed shearing machine high speed shear 30 minutes, add 400 gram sial molecular proportions then and be 30 ZSM-5 molecular sieve, high speed shear is 30 minutes again; Aluminium colloidal sol 500 grams that add salic 20 weight % then; Continue high speed shear 30 minutes, and added 1 gram Triammonium citrate again, continue high speed shear after 30 minutes; With the granularity of this suspension of laser particle analyzer mensuration, its average grain diameter is 2 microns.Use the spray dryer spray shaping, the spray shaping condition is: 240 ℃ of inlet temperatures, and 120 ℃ of outlet temperatures, 10000 rev/mins of centrifugal rotational speeds, exit whirlwind pressure reduction is 0.7KPa, charging rate is 1 kilogram/hour.Particle behind the spray shaping adopts temperature-programmed calcination, burns 3 hours at 400 ℃, and 650 ℃ were burnt 3 hours then.The catalyst that obtains after the roasting is measured granularity with laser particle analyzer, and its average grain diameter is 68 microns, and specific area is 305m
2/ gram, average pore size is 3.2nm, density of catalyst be at 0.9 grams per milliliter, adopt abrasion appearance mensuration abrasion index be 0.001 weight %/hour.
[embodiment 2～10]
According to the method for embodiment 1, adopt the batching and the preparation condition of table 1, wherein Ludox is for containing silica 40 weight %, and it is as shown in table 1 to make the fluid catalyst performance.
[embodiment 11]
The method of getting 200 gram embodiment 1 makes fluid bed ZSM-5 catalyst, puts into internal diameter and be 50 millimeters fluidized-bed reactor, and the component that adopts Shanghai Gaoqiao petro-chemical corporation to produce is C
4～C
10Light oil be raw material (the raw material physical index is seen table 3), the examination activity of such catalysts, range of reaction temperature is 680 ℃, reaction pressure is 0.02MPa, weight space velocity is 1 hour
-1, water/feedstock oil weight ratio is 1: 1 time examination, and obtaining the weight ethylene yield is 27%, and the propylene weight yield is 22%, and diene weight total recovery is 49%.
Table 3 light oil raw material index
| Project | Data |
| Density (20 ℃) kilogram/rice 3 | 704.6 |
| Boiling range is boiling range ℃ just | 40 |
| Whole boiling range ℃ | 160 |
| Saturated vapor pressure (20 ℃) kPa | 50.2 |
| Alkane % (weight %) | 65.2 |
| Cycloalkane % (weight %) | 28.4 |
| Alkene % (weight %) | 0.2 |
| Aromatic hydrocarbons % (weight %) | 6.2 |
Claims (9)
1. fluid catalyst in the finished catalyst weight percentage after the roasting, comprises that following material forms:
A.10～60% molecular sieve;
B.2～40% binding agent;
C.10～60% matrix;
D.0.1～30% anti-wear agent;
Wherein, anti-wear agent is for being selected from bar-shaped or the needle inorganic material, and its draw ratio is 2～20.
2. fluid catalyst according to claim 1; It is characterized in that anti-wear agent is at least a inorganic material that is selected from asbestos, ceramic fibre, glass fibre, the wollastonite mineral; The draw ratio of anti-wear agent is 3～10; In the finished catalyst weight after the roasting, anti-wear agent content is 1～15%.
3. fluid catalyst according to claim 1; It is characterized in that at least a in ZSM-5, modenite, β zeolite, Y zeolite, MCM-22, ZSM-5/ modenite, ZSM-5/ β zeolite or ZSM-5/Y zeolite of molecular screening; The crystal particle diameter of molecular sieve is between 0.1～20um; The density of molecular sieve is at 0.5～2 grams per milliliter, and in the finished catalyst weight after the roasting, molecular sieve content is 20～50%.
4. fluid catalyst according to claim 1; It is characterized in that host material is to be selected from least a in kaolin, calcined kaolin, diatomite, bentonite, carclazyte or the clay; In the finished catalyst weight after the roasting, matrix material content is 15～50%; Binding agent is to be selected from least a in Ludox or the aluminium colloidal sol, and in the finished catalyst weight after the roasting, binder content is 5～20%.
5. the preparation method of a fluid catalyst, may further comprise the steps: (a) molecular sieve, binding agent, host material, expanding agent, dispersant and liquid medium are evenly disperseed to form suspension, the suspension solids content is 10～50%; (b) adopt in the method control suspension of high speed shear or circulating emulsion raw meal particle size between 0.5～5um; (c) in suspension, add anti-wear agent, stir again; (d) this suspension of spray-drying forms microspherical catalyst; (e) this microspherical catalyst of roasting forms finished catalyst.
6. the preparation method of fluid catalyst according to claim 5; It is characterized in that expanding agent is to be selected from least a in methylcellulose, polyvinyl alcohol, sesbania powder, soluble starch or the CNT; In contained molecular sieve weight in the finished catalyst weight after the roasting, the consumption of expanding agent is 1～10%.
7. the preparation method of fluid catalyst according to claim 5; It is characterized in that dispersant is to be selected from least a in Triammonium citrate, ammonium oxalate, ammonium carbonate, the carbonic hydroammonium; In contained molecular sieve weight in the finished catalyst weight after the roasting, the consumption of dispersant is 0.01～10%.
8. the preparation method of fluid catalyst according to claim 5; It is characterized in that the spray shaping condition is 180～350 ℃ of inlet temperatures; 100～180 ℃ of outlet temperatures; 5000～15000 rev/mins of centrifugal rotational speeds, exit whirlwind pressure reduction is 0.5～1.0KPa, charging rate is 0.5～5 kilogram/hour.
9. the preparation method of fluid catalyst according to claim 5; The catalyst of spray-drying preparation is through after the high-temperature roasting; The average grain diameter of particle is between 50～90um, and specific area is between 100～300, and average pore size is between 1～20nm; Density between 0.7～1.4 grams per milliliter, abrasion index 0.001～1.0 weight %/hour.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102615445A CN102371167A (en) | 2010-08-23 | 2010-08-23 | Fluidized bed catalyst and its preparation method |
| PCT/CN2011/001408 WO2012024896A1 (en) | 2010-08-23 | 2011-08-23 | Non-adhesive molecular sieve catalyst and preparation method therefor |
| RU2013112852/04A RU2565599C2 (en) | 2010-08-23 | 2011-08-23 | Binder-free molecular sieve-based catalyst and method for production thereof |
| US13/818,295 US9861969B2 (en) | 2010-08-23 | 2011-08-23 | Binderless molecular sieve catalyst and a preparation method thereof |
| BR112013004126A BR112013004126A2 (en) | 2010-08-23 | 2011-08-23 | binder-free molecular sieve catalyst and method for preparing the same |
| SG2013012976A SG187927A1 (en) | 2010-08-23 | 2011-08-23 | Non-adhesive molecular sieve catalyst and preparation method therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102615445A CN102371167A (en) | 2010-08-23 | 2010-08-23 | Fluidized bed catalyst and its preparation method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102371167A true CN102371167A (en) | 2012-03-14 |
Family
ID=45790721
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102615445A Pending CN102371167A (en) | 2010-08-23 | 2010-08-23 | Fluidized bed catalyst and its preparation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102371167A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103120857A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Solid-liquid separation method of nanometer material |
| CN104549449A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Wear-resistant catalytic cracking fluidized bed catalyst and preparation method thereof |
| CN104888842A (en) * | 2015-05-11 | 2015-09-09 | 中国石油天然气股份有限公司 | Catalytic cracking catalyst, preparation method therefor and application thereof |
| CN106179482A (en) * | 2016-07-01 | 2016-12-07 | 中国华能集团公司 | A kind of method that can fluidize molecular sieve based on vibrations embedding pelletize preparation |
| CN104549296B (en) * | 2013-10-28 | 2017-09-15 | 中国石油化工股份有限公司 | Microspheroidal synthesis gas directly prepares catalyst of low-carbon alkene and preparation method thereof |
| CN107971024A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The preparation method of fluid catalyst |
| CN108067300A (en) * | 2017-12-20 | 2018-05-25 | 卓悦环保新材料（上海）有限公司 | A kind of forming method of SAPO-34 molecular sieve catalysts |
| CN108262069A (en) * | 2017-01-04 | 2018-07-10 | 中国石油化工股份有限公司 | The preparation method of fluid catalyst, the catalyst prepared and its purposes |
| CN109701633A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | Fluid catalyst, preparation method and its usage |
| CN114100567A (en) * | 2021-06-30 | 2022-03-01 | 山东亮剑环保新材料有限公司 | Preparation method of porous spherical molecular sieve VOCs adsorbent |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1704163A (en) * | 2004-05-28 | 2005-12-07 | 中国石油化工股份有限公司 | Molecular screen microspherical catalyst |
| CN101172242A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Catalytic cracking catalyst and its preparation |
| CN101422728A (en) * | 2008-12-18 | 2009-05-06 | 哈尔滨工业大学 | Catalyst for denitration of power plant soot fume SCR and preparation method thereof |
| CN101612592A (en) * | 2009-07-21 | 2009-12-30 | 上海化工研究院 | A kind of preparation method of low abrasion microsphere catalyst produced in situ |
-
2010
- 2010-08-23 CN CN2010102615445A patent/CN102371167A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1704163A (en) * | 2004-05-28 | 2005-12-07 | 中国石油化工股份有限公司 | Molecular screen microspherical catalyst |
| CN101172242A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Catalytic cracking catalyst and its preparation |
| CN101422728A (en) * | 2008-12-18 | 2009-05-06 | 哈尔滨工业大学 | Catalyst for denitration of power plant soot fume SCR and preparation method thereof |
| CN101612592A (en) * | 2009-07-21 | 2009-12-30 | 上海化工研究院 | A kind of preparation method of low abrasion microsphere catalyst produced in situ |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103120857B (en) * | 2011-11-18 | 2015-08-12 | 中国石油化工股份有限公司 | The solid-liquid separating method of nano material |
| CN103120857A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Solid-liquid separation method of nanometer material |
| CN104549449A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Wear-resistant catalytic cracking fluidized bed catalyst and preparation method thereof |
| CN104549449B (en) * | 2013-10-28 | 2017-02-15 | 中国石油化工股份有限公司 | Wear-resistant catalytic cracking fluidized bed catalyst and preparation method thereof |
| CN104549296B (en) * | 2013-10-28 | 2017-09-15 | 中国石油化工股份有限公司 | Microspheroidal synthesis gas directly prepares catalyst of low-carbon alkene and preparation method thereof |
| CN104888842B (en) * | 2015-05-11 | 2017-12-05 | 中国石油天然气股份有限公司 | A kind of catalytic cracking catalyst and preparation method and application |
| CN104888842A (en) * | 2015-05-11 | 2015-09-09 | 中国石油天然气股份有限公司 | Catalytic cracking catalyst, preparation method therefor and application thereof |
| CN106179482B (en) * | 2016-07-01 | 2019-05-17 | 中国华能集团公司 | A method of molecular sieve can be fluidized by embedding to be granulated to prepare based on vibration |
| CN106179482A (en) * | 2016-07-01 | 2016-12-07 | 中国华能集团公司 | A kind of method that can fluidize molecular sieve based on vibrations embedding pelletize preparation |
| CN107971024A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The preparation method of fluid catalyst |
| CN108262069A (en) * | 2017-01-04 | 2018-07-10 | 中国石油化工股份有限公司 | The preparation method of fluid catalyst, the catalyst prepared and its purposes |
| CN108262069B (en) * | 2017-01-04 | 2021-06-22 | 中国石油化工股份有限公司 | Method for producing a fluidized bed catalyst, catalyst produced and use thereof |
| CN109701633A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | Fluid catalyst, preparation method and its usage |
| CN109701633B (en) * | 2017-10-26 | 2022-04-05 | 中国石油化工股份有限公司 | Fluidized bed catalyst, preparation method and application thereof |
| CN108067300A (en) * | 2017-12-20 | 2018-05-25 | 卓悦环保新材料（上海）有限公司 | A kind of forming method of SAPO-34 molecular sieve catalysts |
| CN108067300B (en) * | 2017-12-20 | 2021-01-26 | 卓悦环保新材料（上海）有限公司 | Method for forming SAPO-34 molecular sieve catalyst |
| CN114100567A (en) * | 2021-06-30 | 2022-03-01 | 山东亮剑环保新材料有限公司 | Preparation method of porous spherical molecular sieve VOCs adsorbent |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102371167A (en) | Fluidized bed catalyst and its preparation method | |
| CN102371168B (en) | Preparation method of fluid catalyst | |
| US9861969B2 (en) | Binderless molecular sieve catalyst and a preparation method thereof | |
| CN102372571B (en) | Method for producing propylene by oxygen-containing compound conversion | |
| CN102527445B (en) | Preparation method of low-abrasion fluidized bed microspherical catalyst | |
| CN102372534B (en) | Method for preparing light olefins through conversion of oxygen-containing compounds | |
| CN102372553B (en) | Method for producing olefin by catalytically cracking | |
| CN107971024B (en) | Preparation method of fluidized bed catalyst | |
| EP2430124B1 (en) | Improved catalyst/biomass mixing in transport reactor | |
| CN100413586C (en) | Molecular screen microspherical catalyst | |
| CN108097303B (en) | Preparation method of catalyst for preparing low-carbon olefin by catalytic cracking of diesel oil | |
| CN103962169B (en) | It is a kind of for preparing catalyst of alkene and preparation method thereof by methanol in fluid bed | |
| CN102371183B (en) | Preparation method for adhesive-free fluidized bed catalyst | |
| CN102464548B (en) | Method for preparing propylene by disproportionating fluidized bed olefin | |
| CN102372551B (en) | Method for producing light olefin by catalytically cracking | |
| CN102371175B (en) | Preparation method for adhesive-free ZSM-5/ mordenite fluidized bed catalyst | |
| CN102373070B (en) | Method for producing light olefins by light oil catalytic cracking | |
| CN102371166A (en) | Preparation method of binder-free ZSM-5 fluidized bed catalyst | |
| CN103623858A (en) | Catalytic cracking catalyst and preparation method | |
| CN102373071B (en) | Method for preparing olefins by catalytic pyrolysis | |
| JP2015528744A (en) | Magnesium stabilized ultra-low soda decomposition catalyst | |
| CN104549455B (en) | The method of catalyst of naphtha catalytic cracking production propylene and preparation method thereof and naphtha catalytic cracking production propylene | |
| CN102649086B (en) | Catalyst used in preparation of ethylene through ethanol dehydration | |
| CN102085468B (en) | Pre-fluidizing agent for fluidized bed | |
| CN109701633A (en) | Fluid catalyst, preparation method and its usage |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20120314 |