CN101829592B - Preparation method of fluidizing, catalyzing and cracking catalyst with high solid content - Google Patents
Preparation method of fluidizing, catalyzing and cracking catalyst with high solid content Download PDFInfo
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- CN101829592B CN101829592B CN2009100794289A CN200910079428A CN101829592B CN 101829592 B CN101829592 B CN 101829592B CN 2009100794289 A CN2009100794289 A CN 2009100794289A CN 200910079428 A CN200910079428 A CN 200910079428A CN 101829592 B CN101829592 B CN 101829592B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/061—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing metallic elements added to the zeolite
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/80—Mixtures of different zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0027—Powdering
- B01J37/0036—Grinding
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0027—Powdering
- B01J37/0045—Drying a slurry, e.g. spray drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/42—Addition of matrix or binder particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/084—Y-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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- Crystallography & Structural Chemistry (AREA)
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Abstract
The invention provides a clean and high-efficiency preparation method of an FCC (Fluidizing, Catalyzing and Cracking) catalyst with high solid content. The preparation method comprises the following steps of: pulping clay, molecular sieve slurry, an aluminum-contained adhesive, pseudoboehmite, and the like and evenly mixing into catalyst slurry; aging at a certain temperature; and finally, homogenizing, spraying and drying to obtain a catalyst. The invention is characterized in that pseudoboehmite acidified by inorganic acid is not added in a preparation process; the pseudoboehmite is softened by free H+ ions in the preparation system and is mechanically and physically dispersed at a high speed so that the material granularity D[V, 0.5] is not more than 4 microns, and the influence of the pseudoboehmite on the abrasion index of the catalyst is lessened. The invention can improve the solid content of the catalyst slurry by more than 45m percent, greatly improve the production efficiency of the catalyst, decrease the production cost and lessens the environmental pollution of acidic gases. Meanwhile, the prepared catalyst has higher pore volume and microreactor activity and improved comprehensive reaction performance.
Description
Technical field
The present invention relates to fluid catalytic cracking (FCC) Preparation of catalysts method, be specifically related to a kind of preparation method of highly filled fluidized catalytic cracking catalyst.
Technical background
Fluid catalytic cracking (FCC) technology is the main process of crude oil secondary operations, is the important means that vehicle fuel is produced in domestic and international heavy oil deep processing.Along with the heaviness that processes raw material, inferiorization degree increase the weight of and the vehicle fuel demand rises, the required FCC catalyst consumption amount of this technology is in continuous increase; Owing to the demand of processing heavy oil and the development of FCC technology, the ratio of molecular sieve active component in the FCC catalyst also presents increase trend simultaneously.Usually, the technical process for preparing semi-synthetic FCC catalyst is that raw materials such as binding agent (like aluminium colloidal sol), boehmite, clay, inorganic acid and molecular sieve are processed slurries, obtains catalyst prod through spray shaping and post processing.But this technology exists the colloid solid content before the catalyst spray shaping low; The molecular sieve active component is mixed outstanding problems such as inhomogeneous with other component (being called matrix components); Cause that the Catalyst Production cost is high, moulding microsphere particle size is inhomogeneous, sphericity difference and catalyst active center's poor heat stability, can not give full play to the reactivity worth of molecular sieve in the catalyst.Therefore, people have developed high solids content FCC Preparation of catalysts method.
USP4476239 and USP4443553 have reported a kind of preparation method of Cracking catalyst, it is characterized in that in catalyst slurry, adding dispersant [Al
2(OH)
6-yCl
y]
xOr Al
2(OH)
5NO
3, reduce the viscosity of catalyst slurry, thereby improve the solid content of catalyst spray slurry.In this patent, contain the catalyst slurry of aluminium base binding agent, clay, silicon source and molecular sieve, the solid content of catalyst slurry is 20～25% when not adding dispersant, and the solid content that adds said dispersant rear catalyst slurries can increase to 30%.Its preparation flow is: in agitated reactor, add chemical water and boehmite successively; Add inorganic acid after the making beating evenly again and carry out the reaction of acidifying peptization; Reaction adds kaolin and molecular sieve pulp after finishing successively, and making beating mixes back adding poly ammonium silicate and disperses, and reduces the catalyst slurry fluid viscosity; With gained catalyst slurry spray-drying, obtain the catalyst finished product.
CN1032498A has introduced a kind of preparation method of semi-synthetic fluidized cat catalytic cracking catalyst; Promptly before the catalyst drying; The polyacrylamide that in spray slurry, adds the molecular weight account for catalyst contents on dry basis 0.01～0.15% and be 250～5,000,000 units is as dispersant, and this method can guarantee to reduce catalyst slurry fluid viscosity 10～50% under the impregnable prerequisite of catalyst performance; Not only improved the solid content of aqueous slurry thus greatly; Improve drying efficiency, saved energy consumption, and significantly reduced the bonding phenomenon of material on tube wall and the spray-drying installation inwall.
CN1081219C discloses a kind of method that improves catalyst spray slurry solid content; This method comprises pulls an oar molecular sieve pulp, aluminium colloidal sol, boehmite, clay and inorganic acid; It is characterized in that molecular sieve added before clay and inorganic acid; Inorganic acid adds after aluminium colloidal sol, and preferably inorganic acid adds after aluminium colloidal sol and boehmite.This method can obviously improve the solid content (being up to 45m%) of spray-drying procatalyst slurries, shortens gelation time, thereby improves Catalyst Production efficient, and reduces energy consumption and production costs.
CN1081218C discloses a kind of method that improves catalyst spray slurry solid content; This method comprises pulls an oar molecular sieve pulp, aluminium glue, boehmite, clay and inorganic acid; The solid content that makes slurries is 25～45%; It is characterized in that aluminium colloidal sol added before clay and inorganic acid, molecular sieve pulp adds after inorganic acid, and preferably inorganic acid adds after aluminium colloidal sol and boehmite.This method also can improve the solid content of spray-drying procatalyst slurries.
CN1362472A discloses a kind of preparation method of Cracking catalyst, comprises molecular sieve pulp, boehmite, clay and inorganic acid making beating are mixed, and adds or does not add aluminium colloidal sol, processes catalyst slurry, then spray-drying; It is characterized in that making the amount of boehmite inorganic acid that peptization adds serves as the control index with the catalyst slurry fluid viscosity, the addition of hydrochloric acid so that the catalyst slurry viscosity Control be as the criterion in 10000～100000cp scope.The method that this patent provides is compared with existing technology, can avoid because the catalyst strength that the fluctuation of boehmite acid consumption causes and the fluctuation of pore volume, and the catalyst solid content is 25～52m%.
CN1270203A discloses a kind of preparation method of Cracking catalyst, and this method comprises molecular sieve pulp, aluminium colloidal sol, boehmite, clay and inorganic acid making beating mixed processes catalyst slurry, then spray-drying; It is characterized in that molecular sieve and/or aluminium colloidal sol added before clay and inorganic acid, inorganic acid adds after aluminium colloidal sol, and the addition sequence of rest materials has no particular limits, and contains a kind of viscosity reductant in the said catalyst slurry; Wherein said viscosity reductant is ammonium phosphate, diammonium hydrogen phosphate or ammonium dihydrogen phosphate (ADP), or their mixture, and the addition of viscosity reductant is 0.1～2% of a catalyst butt weight; The weight ratio of Al2O3 in said inorganic acid and the boehmite is 0.02～0.25; The solid content of said catalyst slurry is 30～55 weight %.Method provided by the invention is compared with the method for prior art, can improve the solid content of spray-drying procatalyst slurries greatly, shortens gelation time, thereby improves the production efficiency of catalyst, and reduces energy consumption and production costs.
Though above-mentioned patented method has improved the colloid solid content before the FCC catalyst spray shaping to a certain extent; Be about 25～50m%; But common characteristic is in the preparation process, must add inorganic acid after the adding boehmite boehmite is carried out the reaction of acidifying peptization; Thereby there is following problem inevitably: 1) after boehmite, add owing to inorganic acid; Reaction between inorganic acid and the boehmite is difficult to even generation, always has the local excessive reacting phenomenon, causes slurry viscosity to increase sharply; 2) add fashionable earlier when molecular sieve pulp; Local failure molecular sieve phenomenon can take place in the inorganic acid that the back adds; Because system acidity can not be controlled too low (general pH is greater than 2.8), boehmite is difficult to abundant refinement, especially when molecular sieve content is higher simultaneously; The wear strength variation of catalyst, serviceability is greatly affected; 3) the adding severe corrosion equipment of inorganic acid, the sour gas that produces during simultaneous spray drying produce surrounding environment and pollute.
Summary of the invention
The present invention provides a kind of novel high solids content FCC method for preparing catalyst; Promptly in catalyst preparation process, do not add inorganic acid and carry out the acidification pseudo-boehmite reaction; But adopt the method for mechanical-physical high speed dispersion that it is carried out dispersing and disintegrating; Efficiently solve of the influence of boehmite peptization state, can improve the preceding colloid solid content of catalyst spray shaping, realize FCC catalyst clean productive target efficiently catalyst solid content and abrasion index.
High solids content FCC method for preparing catalyst provided by the invention is: will prepare the required various materials of catalyst; Mainly comprise deionized water, clay, molecular sieve pulp, contain al binder, boehmite, dispersant add agitated reactor; Making beating mixes processes catalyst slurry; At 25～80 ℃ of following aging reaction 10min～100min, last homogeneous spray-drying makes high solids content FCC catalyst then.Technical characterictic of the present invention is that boehmite adds agitated reactor after aluminium colloidal sol; And the 20min～120min that fully pulls an oar, afterwards with mechanical approach with the boehmite high speed dispersion, make boehmite granularity D [V; 0.5] be not more than 4 μ m, reduce its influence to the catalyst abrasion index.This method does not limit the rest materials addition sequence.The composition of catalyst slurry (according to catalyst butt quality meter) is molecular sieve 15～50m%, clay 15～60m%, and boehmite 8～30m% contains al binder (by aluminium oxide) 3～18m%, and the gained slurry solid content is 35～55m%.Said catalyst slurry can also contain one or more oxides that are selected from rare earth oxide, zinc oxide, silica, magnesia, titanium oxide, vanadium oxide, cupric oxide or its predecessor of 0～8m%; Wherein preferably rare earth oxide, silica or their predecessor.
High solids content FCC method for preparing catalyst provided by the invention, said molecular sieve are one of y-type zeolite (comprising various modified zeolite of Y-type) or y-type zeolite and ZSM zeolite, β zeolite, omega zeolite, MCM zeolite, SAPO zeolite or several mixtures; The wherein preferred y-type zeolite or the mixture of y-type zeolite and ZSM-5 zeolite.Wherein said modified zeolite of Y-type is a kind of of HY, NH4Y, REY, USY, REUSY, other element modified Y zeolite, perhaps their mixture.
The said clay of high solids content FCC method for preparing catalyst provided by the invention is a kind of in kaolin, sepiolite, galapectite, the imvite or their mixture; Wherein preferred kaolin, galapectite or their mixture; Kaolin most preferably.
The said boehmite of high solids content FCC method for preparing catalyst provided by the invention can be boehmite, three boehmites, bayerite, preferably boehmite.
The al binder that contains of the present invention comprises aluminium colloidal sol, aluminium chloride, sour modified kaolin, can obtain through one of following approach:
(1) metallic aluminium adds hydrochloric acid (or aluminium chloride) reaction
(2)] crystal aluminum chloride pyrolytic process
(3) inorganic acid and kaolin or roasting kaolin react
(4) other approach is as reacting hydrochloric acid and aluminium hydroxide under pressure
The preferred version of high solids content FCC method for preparing catalyst provided by the invention is: aluminium colloidal sol adds in all material prior, and boehmite added before molecular sieve.As will contain al binder and chemical water adding agitated reactor earlier, then after wherein adding clay and boehmite, stirring; High speed dispersion is to raw meal particle size [V; 0.5] be not more than 4 μ m, add molecular sieve pulp again, mix the back and add dispersant; Aging 10min～the 100min of intensification makes catalyst with gained slurries spray-drying then.
High solids content FCC method for preparing catalyst provided by the invention can also be: will contain al binder and deionized water earlier and add agitated reactor, and add boehmite then and relax reaction 20min～120min, high speed dispersion is to raw meal particle size [V; 0.5] be not more than 4 μ m, add molecular sieve and clay at last, after stirring; Add dispersant; Stir, the aging 10min～100min that heats up then makes catalyst with gained slurries spray-drying.
High solids content FCC method for preparing catalyst provided by the invention can also be: will contain al binder and deionized water earlier and add agitated reactor; Add boehmite then and relax reaction 20min～120min; High speed dispersion to raw meal particle size [V, 0.5] is not more than 4 μ m, and aging 10min～100min then heats up; Add molecular sieve and clay at last, after stirring gained slurries spray-drying is made catalyst.
For adopting boehmite and the semi-synthetic FCC catalyst that contains the compound preparation of al binder, the existence of boehmite is the key factor that influences catalyst slurry fluid solid content height and catalyst wear strength.Key problem in technology of the present invention is an existence of putting forth effort to control boehmite, in catalyst preparation process, does not add the inorganic acid acidification pseudo-boehmite, but utilizes the free H of Preparation of Catalyst system
+Ion softens the boehmite surface, consumes free H
+Ion reduces H
+Ion to the destruction of molecular sieve, improves the initial cracking activity of catalyst when spray-drying; In the preparation process, softening boehmite particle being carried out mechanical-physical simultaneously disperses; Reduce its influence to the catalyst abrasion index; And make it fully to mix with other components, increased the active coordinating protection effect of matrix components to molecular sieve component.Therefore; Compared with prior art; Do not influencing under the mobile prerequisite of catalyst slurry; Can be increased to 35m%～55m% according to the prepared catalyst slurry fluid solid content of high solids content FCC method for preparing catalyst provided by the invention, gained catalyst physicochemical property and reactivity worth do not receive negative effect.The enforcement of this technology can significantly improve the production efficiency of catalyst, reduces the pollutant discharge amount in the production process, and reduces catalyst flash distillation energy consumption and production cost.Evaluation result shows, adopts the FCC catalyst of this technology preparation to have open middle macropore pore passage structure, the heavy oil conversion performance of catalyst be improved significantly, increased the yield of high value added product.
The specific embodiment
Following instance is further described characteristics of the present invention, but protection scope of the present invention does not receive the restriction of these instances.
In each instance, adopt the viscosity of Cole Parmer98936-15 rotary viscosity measuring slurries, measuring condition is: rotating speed 20rpm, rotating shaft R4; The measuring method of gained catalyst physical and chemical index is as shown in table 1.
Table 1 catalyst analysis assessment method
| Project | Method | Standard No. |
| Pore volume mLg -1 | The water droplet method | Q/SYLS?0521-2002 |
| Abrasion index m% | The gas lift method | Q/SYLS?0518-2002 |
| Micro-activity (800 ℃, 17 hours) m% | Miniature fixed bed reaction | Q/SYLS?0589-2002 |
| Reaction selectivity | Fixed fluidized bed reaction | Q/SYLS?0641-2002 |
| Octane number | Chromatography | M213·02-07-2003 |
| Gasoline is formed v% | Chromatography | Beijing Shi Keyuan software |
Raw materials used specification is following in the instance:
1.1
#Boehmite (the peptization index is not less than 95% for Shandong Aluminum Plant, igloss 39.6%), 2
#Boehmite (the peptization index is not less than 95% for Shanxi Aluminium Plant, igloss 40.4%), kaolin (igloss 25.4%, kaolinite content is not less than 85%), galapectite (igloss 19.2%, galapectite is not less than 90%); Aluminium colloidal sol (salic 23.0%); Rare earth chloride (rare earth oxide content is 308.75g/L), waterglass (silicon oxide-containing 250g/L) is industrial certified products, picks up from Catalyst Factory of Lanzhou Petrochemical Company.
2.USY molecular sieve (igloss 4.8%, cell parameter a
oBe 2.452nm), REUSY molecular sieve (igloss 5.3%, rare earth oxide 8.5%, cell parameter a
oBe 2.462nm), REY (igloss 4.4%, rare earth oxide 18.1%), be qualified industrial goods, pick up from Catalyst Factory of Lanzhou Petrochemical Company; High silica ZSM-5 (igloss 5.1%, silica alumina ratio is greater than 300), industrial certified products, Fudan University in Shanghai production.
Embodiment 1
In agitated reactor, add rare earth chloride, 1441 gram aluminium colloidal sols and the 1284 gram 1# boehmites of 573 gram deionized waters, 32ml, the mixing making beating is dispersed to raw meal particle size [V, 0.5] with high speed dispersor again after 60 minutes and equals 3 μ m; Add 1852 gram kaolin afterwards, stirred 30 minutes, add again afterwards with colloid mill is levigate and restrain the β zeolites and restrain the molecular sieve pulp that deionized waters mix to 1384 gram REUSY molecular sieves, the 19 gram ZSM-5 of Fudan University molecular sieves, 48 of average grain diameter with 2615 less than 5 microns; Stir be warming up to after 1 hour 60 ℃ aging 60 minutes; The homogeneous spray-drying 500 ℃ of roastings 0.5 hour, adds 8 times of deionized waters with gained catalyst microballoon then then; Stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-1.
The solid content of catalyst A-1 spray slurry is 43.5w%, and slurry viscosity is 4058 centipoises, and the abrasion index of gained catalyst is 1.5, and pore volume is 0.43mLg
-1, micro-activity 65.
Embodiment 2
In agitated reactor, add 929 gram deionized waters, 1622 gram aluminium colloidal sols, 1156 grams 1
#Boehmite and 1902 gram kaolin mixed making beating after 60 minutes, were dispersed to raw meal particle size [V with high speed dispersor again; 0.5] equal 2 μ m, add again afterwards with colloid mill is levigate and restrain the molecular sieve pulp that deionized waters mix less than 5 microns 1573 gram REUSY molecular sieves, the 43 gram ZSM-5 of Fudan University molecular sieves and 2468 to average grain diameter, add the waterglass of 13ml again; Stir be warming up to after 1 hour 60 ℃ aging 120 minutes, homogeneous spray-drying then, with gained catalyst microballoon 500 ℃ of roastings 0.5 hour; Add 8 times of deionized waters then, stir, 80 ℃ of washings 15 minutes; Filtration drying promptly gets the FCC catalyst of the inventive method preparation, and note is A-2.
The solid content of catalyst A-2 spray slurry is 41w%, and slurry viscosity is 4319 centipoises, and the abrasion index of gained catalyst is 1.2, and pore volume is 0.42mLg
-1, micro-activity 65.
Embodiment 3
In agitated reactor, add 3104 gram deionized waters, 1465 gram REUSY molecular sieves and the 43 gram ZSM-5 of Fudan University molecular sieves, add 1261 gram aluminium colloidal sols, 2103 gram kaolin and 963 grams 1 after mixing again successively
#Boehmite stirred after 100 minutes, was dispersed to raw meal particle size [V with high speed dispersor; 0.5] equal 3.6 μ m, be warming up to 70 ℃ then and wore out 40 minutes, then the homogeneous spray-drying; Gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added 8 times of deionized waters then, stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-3.
The solid content of catalyst A-3 spray slurry is 44.2w%, and slurry viscosity is 4835 centipoises, and the abrasion index of gained catalyst is 1.6, and pore volume is 0.43mLg
-1, micro-activity 64.
Embodiment 4
In agitated reactor, add 1782 gram deionized waters, 1662 gram aluminium colloidal sols and 2003 gram kaolin successively, add 1091 grams 1 after mixing again
#Boehmite, the mixing making beating is dispersed to raw meal particle size [V, 0.5] with high speed dispersor again after 80 minutes and equals 1.5 μ m; Add again afterwards with colloid mill is levigate and restrain the molecular sieve pulp that deionized waters mix less than 5 microns 814 gram USY molecular sieves, the REUSY of 629 grams, the 43 gram ZSM-5 of Fudan University molecular sieves, 18 gram β zeolites with 2482 to average grain diameter; The waterglass that adds 79ml again, stir be warming up to after 1 hour 40 ℃ aging 80 minutes, homogeneous spray-drying then; With gained catalyst microballoon 500 ℃ of roastings 0.5 hour; Add 8 times of deionized waters then, stir, 80 ℃ of washings 15 minutes; Filtration drying promptly gets the FCC catalyst of the inventive method preparation, and note is A-4.
The solid content of catalyst A-4 spray slurry is 38w%, and slurry viscosity is 3549 centipoises, and the abrasion index of gained catalyst is 0.8, and pore volume is 0.40mLg
-1, micro-activity 65.
Embodiment 5
The REUSY molecular sieve that in agitated reactor, adds 1871 gram deionized waters, 326 gram USY molecular sieves and 764 grams adds 1622 gram aluminium colloidal sols, 2603 gram kaolin and 899 grams 1 more successively after mixing
#Boehmite stirred after 30 minutes, was dispersed to raw meal particle size [V with high speed dispersor; 0.5] equal 2.5 μ m, be warming up to 80 ℃ then and wore out 15 minutes, then the homogeneous spray-drying; Gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added 8 times of deionized waters then, stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-5.
The solid content of catalyst A-5 spray slurry is 49w%, and slurry viscosity is 5327 centipoises, and the abrasion index of gained catalyst is 1.0, and pore volume is 0.44mLg
-1, micro-activity 65.
Embodiment 6
In agitated reactor, add 1918 gram deionized waters, 1124 gram REUSY molecular sieves, add 901 gram aluminium colloidal sols, 2904 gram kaolin and 770 grams 2 after mixing again successively
#Boehmite stirred after 40 minutes, was dispersed to raw meal particle size [V with high speed dispersor; 0.5] equal 2.0 μ m, be warming up to 50 ℃ then and wore out 40 minutes, then the homogeneous spray-drying; Gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added 8 times of deionized waters then, stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-6.
The solid content of catalyst A-6 spray slurry is 52w%, and slurry viscosity is 4905 centipoises, and gained catalyst abrasion index is 1.4, and pore volume is 0.43mLg
-1, micro-activity 63.
Embodiment 7
In agitated reactor, add 1370 gram deionized waters, 1441 gram aluminium chlorides, 1156 grams 2
#Boehmite, 1502 gram kaolin and 535 gram galapectites mixed making beating after 70 minutes, were dispersed to raw meal particle size [V with high speed dispersor again; 0.5] equal 2.0 μ m, add again afterwards with colloid mill is levigate and restrain the molecular sieve pulp that deionized waters mix less than 5 microns 1528 gram REUSY molecular sieves, the 43 gram ZSM-5 of Fudan University molecular sieves with 2397 to average grain diameter, stir and be warming up to 70 ℃ after 1 hour and wore out 50 minutes; The homogeneous spray-drying 500 ℃ of roastings 0.5 hour, adds 8 times of deionized waters with gained catalyst microballoon then then; Stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-7.
The solid content of catalyst A-7 spray slurry is 40w%, and slurry viscosity is 4195 centipoises, and the abrasion index of gained catalyst is 1.8, and pore volume is 0.42mLg
-1, micro-activity 66.
Embodiment 8
In agitated reactor, add 2637 gram deionized waters, 1483 gram REUSY molecular sieves and the 43 gram ZSM-5 of Fudan University molecular sieves, add rare earth chloride, 2253 gram kaolin and 963 grams 1 of 1261 gram aluminium chlorides, 83ml after mixing again successively
#Boehmite stirred after 100 minutes, was dispersed to raw meal particle size [V with high speed dispersor; 0.5] equal 3.0 μ m, be warming up to 55 ℃ then and wore out 120 minutes, then the homogeneous spray-drying; Gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added 8 times of deionized waters then, stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst of the inventive method preparation, and note is A-8.
The solid content of catalyst A-8 spray slurry is 46w%, and slurry viscosity is 5028 centipoises, and the abrasion index of gained catalyst is 1.5, and pore volume is 0.42mLg
-1, micro-activity 65.
Comparative Examples 1
In agitated reactor, add 1441 gram aluminium colloidal sols and 573 gram deionized waters, when stirring, add 1284 grams 1
#Boehmite, pulling an oar added 1852 gram kaolin in 20 minutes, and stirring to pulp adds 305 after 40 minutes to restrain concentration be 22% hydrochloric acid; Stir after 30 minutes, add levigate with colloid mill to the 1384 gram REUSY molecular sieves of average grain diameter less than 5 microns, the molecular sieve pulp that the 43 gram ZSM-5 of Fudan University molecular sieves mix with 2615 gram deionized waters; Pull an oar and carry out spray-drying after 30 minutes, gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added 8 times of deionized waters then; Stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst, and note is B-1.
The solid content of the spray slurry of catalyst B-1 is 43.2w%, and slurry viscosity is 13092 centipoises, and the abrasion index of gained catalyst is 2.7, and pore volume is 0.40mLg
-1, micro-activity 63.
Data show, the viscosity of catalyst slurry is high, mobile poor when adopting this method to improve solid content, in actual production, also possibly have the catalyst index problem of higher of resistance to wearing; In spray shaping,, reduced the micro-activity of catalyst because of the molecular sieve structure that added sour gas partial destruction that a large amount of hydrochloric acid produces.
Comparative Examples 2
In agitated reactor, add 929 gram deionized waters and 1902 gram kaolin, pull an oar that to add 230 gram concentration after 30 minutes be 35% hydrochloric acid, mixed afterreaction 1 hour, adding 1156 restrains 1 under stirring
#Boehmite, stir be warming up to after back 0.5 hour 70 ℃ aging 1 hour, add 1622 gram aluminium colloidal sols again; Stir after 20 minutes, add, pull an oar and carry out spray-drying after 30 minutes by 1573 gram REUSY molecular sieves, the 43 gram ZSM-5 of Fudan University molecular sieves and the molecular sieve pulp that 2468 gram deionized waters mix; Gained catalyst microballoon 500 ℃ of roastings 0.5 hour, is added deionized water then, stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst, and note is B-2.
The solid content of the spray slurry of catalyst B-2 is 41w%, and slurry viscosity is 12653 centipoises, and the abrasion index of gained catalyst is 1.7, and pore volume is 0.38mLg
-1, micro-activity 62.
Data show, adopt the high solids content catalyst of this method preparation, because the restriction of boehmite peptization state, the catalyst solid content reaches capacity, and slurry viscosity is big, mobile poor, has increased industrial difficulty; Because slurry viscosity is big, molecular sieve mixes inhomogeneous with matrix, cause the catalyst micro-activity on the low side simultaneously.
Comparative Examples 3
In agitated reactor, add with colloid mill be milled to average grain diameter less than 5 microns restrain the slurries that the REUSY molecular sieves are formed by 3065 gram deionized waters with 1628; Adding 1622 gram aluminium colloidal sols; When stirring, add 1522 gram kaolin then, stir adding 1284 grams 1 after 15 minutes
#Boehmite stirs that to add 305 gram concentration in 20 minutes be 22% hydrochloric acid, pulls an oar and carries out spray-drying after 30 minutes; With gained catalyst microballoon 500 ℃ of roastings 0.5 hour; Add 8 times of deionized waters then, stir, 80 ℃ of washings 15 minutes; Filtration drying promptly gets the FCC catalyst, and note is B-3.
The solid content of the spray slurry of catalyst B-3 is 38.7w%, and slurry viscosity is 7248 centipoises, and the abrasion index of gained catalyst is 3.9, and pore volume is 0.41mLg
-1, micro-activity 63.
Data show that when molecular sieve content is higher in the catalyst if adopt this method to improve the catalyst slurry fluid solid content, the index that resistance to wears of catalyst is higher, and the micro-activity of catalyst is on the low side simultaneously.
Comparative Examples 4
In agitated reactor, add 503 gram deionized waters, 1261 gram aluminium colloidal sols and 963 grams 1
#Boehmite, high speed dispersion to raw meal particle size [V, 0.5] equals 7.5 μ m; Add again afterwards and mix back adding 2103 and restrain kaolin to 1465 gram REUSY molecular sieves, the 43 gram ZSM-5 of Fudan University molecular sieves and the molecular sieve pulp that 2691 gram deionized waters mix of average grain diameter, stir and be warming up to 50 ℃ after 1 hour and wore out 60 minutes less than 5 microns with colloid mill is levigate; The homogeneous spray-drying 500 ℃ of roastings 0.5 hour, adds 8 times of deionized waters with gained catalyst microballoon then then; Stir; 80 ℃ of washings 15 minutes, filtration drying promptly got the FCC catalyst, and note is A-3.
The solid content of the spray slurry of catalyst A-3 is 44.2w%, and slurry viscosity is 5638 centipoises, and the abrasion index of gained catalyst is 3.8, and pore volume is 0.40mLg
-1, micro-activity 65.
Data show this method of employing when the boehmite particle diameter is big, and the catalyst abrasion index can not satisfy industrial index.
Table 2 is that the inventive method prepares catalyst and the evaluation result of comparative catalyst on fixed fluidized bed device.500 ℃ of fixed fluidized bed reaction temperatures, oil ratio are 4, air speed 15h
-1, feedstock oil is the decompression residuum that Xinjiang Oil Regions is mixed refining 30%.
The evaluation result of table 2 catalyst on fixed fluidized bed
| Experiment numbers | Embodiment 1 | Comparative Examples 1 | Comparative Examples 3 |
| Catalyst | A-1 | B-1 | B-3 |
| Abrasion index, % | 1.5 | 2.7 | 3.3 |
| Pore volume, mL.g -1 | 0.40 | 0.40 | 0.41 |
| Micro-activity, % | 79 | 77 | 76 |
| Dry gas, % | 1.78 | 1.81 | 1.80 |
| Liquefied gas, % | 16.17 | 16.07 | 15.91 |
| Gasoline, % | 48.64 | 48.10 | 48.30 |
| Diesel oil, % | 17.32 | 17.42 | 17.13 |
| Heavy oil, % | 7.90 | 8.38 | 8.58 |
| Coke, % | 8.03 | 8.00 | 8.15 |
| Amount to % | 99.84 | 99.78 | 99.87 |
| Conversion ratio, % | 74.63 | 73.98 | 74.16 |
| Total liquid is received % | 82.14 | 81.59 | 81.30 |
| Light receipts, % | 65.96 | 65.52 | 65.43 |
| Gasoline olefin, v% | 13.43 | 15.13 | 15.29 |
| ?MON | 81.6 | 81.4 | 81.7 |
| ?RON | 91.5 | 91.9 | 91.6 |
Can know from table 2; Compare with B-3 with the catalyst B-1 of Comparative Examples preparation; The catalyst A-1 of process preparation of the present invention has best heavy oil conversion performance and the highest total liquid is received, and the olefin(e) centent that generates gasoline simultaneously is lower, and the general reaction performance of catalyst improves.
Claims (9)
1. a high solids content preparation method of fluidizing, catalyzing and cracking catalyst with the required material of preparation catalyst, mainly comprises deionized water, clay, molecular sieve pulp, contains al binder and boehmite adding agitated reactor; Making beating mixes processes catalyst slurry; At 25～80 ℃ of following aging reaction 10min～100min, last homogeneous spray-drying makes catalyst through roasting, washing, filtration drying more then; It is characterized in that described boehmite adds agitated reactor after containing al binder; And the 20min～120min that fully pulls an oar, afterwards with mechanical approach with the boehmite high speed dispersion, make boehmite granularity D [V; 0.5] being not more than 4 μ m, other material charging sequence is not limit.
2. according to the described preparation method of claim 1; The composition that it is characterized in that described catalyst slurry contains molecular sieve 15～50m%, clay 15～60m% at least according to butt quality meter; Boehmite 8～30m% contains al binder and counts 3～18m% by aluminium oxide.
3. according to the described preparation method of claim 1, it is characterized in that containing in the described catalyst slurry one or more oxides that are selected from rare earth oxide, zinc oxide, silica, magnesia, titanium oxide, vanadium oxide, cupric oxide or its predecessor of 0～8m%.
4. according to the described preparation method of claim 3, it is characterized in that described catalyst slurry contains rare earth oxide, silica or their predecessor.
5. according to the described preparation method of claim 1, it is characterized in that described molecular sieve is one or more mixtures in y-type zeolite or y-type zeolite and ZSM zeolite, β zeolite, omega zeolite, MCM zeolite, the SAPO zeolite.
6. according to the described preparation method of claim 5, it is characterized in that described molecular sieve is the mixture of y-type zeolite and ZSM-5 zeolite.
7. according to the described preparation method of claim 5, it is characterized in that described y-type zeolite is a modified zeolite of Y-type.
8. according to the described preparation method of claim 1, it is characterized in that described clay is a kaolin.
9. according to the described preparation method of claim 1, it is characterized in that the described al binder that contains is aluminium colloidal sol, aluminium chloride.
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| CN115845906A (en) * | 2022-12-01 | 2023-03-28 | 黄河三角洲京博化工研究院有限公司 | Preparation method of catalyst for heavy oil to produce more light olefins and aromatic hydrocarbons |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5168086A (en) * | 1989-03-02 | 1992-12-01 | W. R. Grace & Co.-Conn. | Catalytic cracking catalysis |
| CN1143666A (en) * | 1996-02-08 | 1997-02-26 | 中国石油化工总公司 | Cracking catalyst for producing isomeric olefine and gasoline with high yield |
| US20030166453A1 (en) * | 2002-02-25 | 2003-09-04 | Kuvettu Mohan Prabhu | Stabilized dual zeolite single particle catalyst composition and a process thereof |
| CN1785518A (en) * | 2004-12-10 | 2006-06-14 | 中国科学院兰州化学物理研究所 | Catalytic cracking catalyst of propylene and ethylene and its preparation method |
| CN101134905A (en) * | 2006-08-30 | 2008-03-05 | 中国石油天然气股份有限公司 | Method for improving solid content of catalytic cracking catalyst slurry |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1081218C (en) * | 1998-09-17 | 2002-03-20 | 中国石油化工集团公司 | Preparation of petroleum cracking catalyst |
-
2009
- 2009-03-10 CN CN2009100794289A patent/CN101829592B/en active Active
- 2009-05-07 WO PCT/CN2009/000500 patent/WO2010102430A1/en active Application Filing
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5168086A (en) * | 1989-03-02 | 1992-12-01 | W. R. Grace & Co.-Conn. | Catalytic cracking catalysis |
| CN1143666A (en) * | 1996-02-08 | 1997-02-26 | 中国石油化工总公司 | Cracking catalyst for producing isomeric olefine and gasoline with high yield |
| US20030166453A1 (en) * | 2002-02-25 | 2003-09-04 | Kuvettu Mohan Prabhu | Stabilized dual zeolite single particle catalyst composition and a process thereof |
| CN1785518A (en) * | 2004-12-10 | 2006-06-14 | 中国科学院兰州化学物理研究所 | Catalytic cracking catalyst of propylene and ethylene and its preparation method |
| CN101134905A (en) * | 2006-08-30 | 2008-03-05 | 中国石油天然气股份有限公司 | Method for improving solid content of catalytic cracking catalyst slurry |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107983399A (en) * | 2017-12-29 | 2018-05-04 | 广东石油化工学院 | A kind of FCC catalysts and preparation method thereof |
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