CN115025806A - Preparation method of iron pollution resistant catalytic cracking catalyst - Google Patents

Preparation method of iron pollution resistant catalytic cracking catalyst Download PDF

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CN115025806A
CN115025806A CN202210543570.XA CN202210543570A CN115025806A CN 115025806 A CN115025806 A CN 115025806A CN 202210543570 A CN202210543570 A CN 202210543570A CN 115025806 A CN115025806 A CN 115025806A
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catalyst
pulping
aluminum
iron
preparation
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钟晓亮
王涛
李世鹏
高明军
谭映临
叶红
张新功
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Qingdao Huicheng Environmental Protection Technology Group Co ltd
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00Catalysts comprising molecular sieves
    • B01J29/04Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/085Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/088Y-type faujasite
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14Phosphorus; Compounds thereof
    • B01J27/16Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0018Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08Heat treatment
    • B01J37/082Decomposition and pyrolysis
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04Oxides
    • C10G11/05Crystalline alumino-silicates, e.g. molecular sieves
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10After treatment, characterised by the effect to be obtained
    • B01J2229/20After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70Catalyst aspects
    • C10G2300/705Passivation

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)

Abstract

The invention discloses a preparation method of an iron pollution resistant catalytic cracking catalyst. The method is to improve the specific surface area and pore volume of the matrix of the catalyst by pore-enlarging modification of kaolin, and simultaneously improve the iron pollution resistance of the catalyst by aluminum-rich and zinc-rich modification on the surface of catalyst particles. The catalyst shows better iron pollution resistance and excellent product selectivity under higher iron loading, thereby providing a convenient and feasible solution for processing crude oil with high iron content.

Description

Preparation method of iron pollution resistant catalytic cracking catalyst
Technical Field
The invention relates to the technical field of catalysts, in particular to a preparation method of an iron pollution resistant catalytic cracking catalyst.
Background
At present, catalytic cracking plays a very important role in the field of petroleum refining as a main means of crude oil secondary processing, and the performance of a catalytic cracking catalyst is a key factor which directly influences product distribution. With the increasing weight and deterioration of crude oil, the metal content in the raw material is increased, and the main metal elements include vanadium and nickel, as well as iron, calcium, sodium, copper and the like. Therefore, higher demands are made on the metal contamination resistance of the catalyst. At present, the research on the resistance to nickel-vanadium pollution is more, but less iron is needed, and two reasonable explanations are summarized for the poisoning mechanism of iron, wherein the first explanation is as follows: iron is similar to other metals such as nickel, vanadium and the like, the iron mainly exists in macromolecular hydrocarbon of the raw material, iron is continuously deposited on the outer surface of particles in the process of carrying out pre-cracking reaction on the macromolecular components of the raw material on a substrate, and is gradually enriched on the outer surface of the particles due to weaker migration activity, so that the pore passages of the substrate are blocked, the accessibility of an active center is reduced, the heavy oil conversion capacity of the catalyst is reduced, and the yield of a target product is poor; the second explanation: the pore channel of the matrix is blocked not only because of the physical deposition of iron, but also because iron can form low-melting-point eutectic with silicon, calcium, sodium and the like in the matrix, the surface of catalyst particles can be in a glass shape in the melting process, a nodular bulge is formed when the temperature is reduced, and a compact shell layer with the diameter of 1-3 mu m is formed on the surface, so that the internal diffusion mass transfer of oil gas molecules is influenced, the number of active centers is greatly reduced, and the fluidization of the catalyst in the device is influenced in severe cases.
Based on the above destruction mechanism, aiming at improving the iron pollution resistance, on one hand, the specific surface area and the pore volume of the catalyst substrate component are increased, the eutectic with low melting point is dispersed, and the blockage of the eutectic to the catalyst pore channel is reduced; on the other hand, the content of the alumina in the catalyst substrate is increased, so that the iron oxide is deposited on the surface of the alumina as much as possible to reduce the generation of low-melting eutectic substances.
At present, the patent technology related to the preparation of the catalyst for resisting iron pollution is few, so that a feasible catalyst preparation process technology is urgently needed, and a feasible catalyst use scheme is provided for processing high-iron crude oil.
CN107303507A discloses a method for preparing alumina containing phosphorus and silicon, the alumina carrier prepared by the method keeps the characteristics of high specific surface area and large pore volume of pseudo-boehmite, and the acid content of the alumina carrier can be simply adjusted within a larger range by using the contents of phosphorus and silicon, so that the carrier can be used in a plurality of fields.
CN102188963A discloses a method for modifying kaolin, which comprises using kaolin as a raw material, first roasting the kaolin at a high temperature, then uniformly stirring the high-temperature roasted kaolin with an additional aluminum source and an acid solution to obtain a mixed slurry, and reacting under certain conditions, and then directly using the mixed slurry as a raw material for preparing a catalytic cracking catalyst without filtering. The modified kaolin has developed medium-large pore volume and certain activity, and the slurry containing the modified kaolin also has certain binding property, so that the catalyst prepared by the slurry containing the modified kaolin has stronger heavy metal resistance.
CN109692694A discloses a macroporous kaolinite, its preparation and application, the macroporous kaolinite contains rare earth, the average pore diameter is 2-50nm, the pore volume of the pore with pore diameter of 10-50nm accounts for more than 80% of the total pore volume. The preparation method of the macroporous kaolinite comprises the following steps: the preparation method comprises the following steps of carrying out first roasting on kaolin, forming a mixture of the kaolin subjected to the first roasting, a first acidic solution and an optional rare earth compound, carrying out first treatment, then carrying out second roasting, mixing the mixture with a second acidic solution, a pore-expanding agent and the optional rare earth compound, carrying out second treatment, filtering and drying to obtain the macroporous kaolinite, wherein the rare earth compound is introduced in at least one of the first treatment and the second treatment. The macroporous kaolinite has high cracking activity, is used for a catalyst cracking catalyst to replace clay, and has the advantages of good coke selectivity, strong heavy metal pollution resistance and high gasoline yield on the premise of equivalent rare earth content.
The invention content is as follows:
the invention discloses a preparation method of an anti-iron pollution catalytic cracking catalyst, aiming at improving the anti-iron pollution capacity of the catalyst and realizing the purpose of stably and efficiently processing high-iron crude oil, and the method comprises the following specific steps:
(1) mixing kaolin and phosphorus-aluminum glue, pulping, controlling the solid content to be more than or equal to 50%, and stirring for more than or equal to 6 hours;
(2) adding polyethylene glycol into the aluminum sol, and stirring for later use;
(3) adding water into pseudo-boehmite for pulping, and adding boric acid for pre-acidification;
(4) adding water into REY molecular sieve, pulping, and stirring for later use;
(5) and (3) mixing the serosity in the steps (1), (2), (3) and (4) in a parallel flow manner, adding hydrochloric acid, controlling the pH value to be 2.2-3.0, and performing spray granulation, roasting, washing and drying to obtain a finished product.
In the step (1), adding P as the proportion of the phosphor-aluminum glue 2 O 5 Accounting for 5-10 wt% of the dry basis of the finished product.
In the step (1), the composition of the phosphor-aluminum paste is P 2 O 5 With Al 2 O 3 The molar ratio is 4.5-10.
In the step (2), the molecular weight of the polyethylene glycol is 1000-2000g/mol, and the adding proportion accounts for Al 2 O 3 0.001-0.01 wt% of the aluminum solution.
In the step (3), the boric acid is added in the proportion of H 3 BO 3 Calculated as Al 2 O 3 0.1-0.3 wt% of pseudoboehmite.
In the step (5), an opening is added on a pipeline connected with the roasting furnace at the bottom of the spraying tower so as to realize the purpose of continuously adding zinc hydroxide, wherein the adding proportion of the zinc hydroxide is 0.1-0.5 wt% of the dry basis of the finished product calculated by ZnO. The innovation points or advantages of the invention are as follows:
(1) firstly, the kaolin is pulped with the phosphor-aluminum glue, and the composition of the phosphor-aluminum glue is P 2 O 5 With Al 2 O 3 The molar ratio is 4.5-10, except for being used as a binder, the pH value of the slurry is lower due to excessive phosphoric acid, the temperature of the slurry is raised by controlling the pulping solid content and the stirring time and the shearing friction of stirring, the two act together to dissolve a small part of alumina of the kaolin into the slurry, pore channels are dredged and widened, and the height is increasedThe specific surface area of ridge soil can effectively reduce the hole plugging effect of iron pollution.
(2) Polyethylene glycol is added into the aluminum sol, so that the dispersion and surface tension of micelles are improved, the slurry is quickly shrunk into a spherical shape in the spray drying process, and the aluminum sol is more dispersed on the outer surface of the particles, so that the aim of enriching aluminum on the surface is fulfilled.
(3) The boric acid pre-acidified pseudo-boehmite can form holes in a certain proportion by utilizing the characteristics of 169 ℃ of melting point (decomposition) and 300 ℃ of boiling point of boric acid during roasting, thereby improving the diffusion performance of the catalyst.
(4) The zinc hydroxide and the catalyst particles enter a roasting furnace together, the zinc hydroxide is decomposed into zinc oxide and water at 125 ℃, the zinc oxide is adsorbed on the surfaces of the catalyst particles, and the zinc oxide and iron can form high-melting-point substances to achieve the purpose of iron fixation, so that the toxicity of the iron is reduced.
(5) The excessive phosphoric acid in the phosphorus-aluminum gel contacts with various substances to form phosphorus hydroxyl, so that the acid center number of the catalyst is increased, and the cracking capability of the catalyst is improved.
Compared with the catalyst prepared by the conventional method, the catalyst prepared by the technical means has higher mesopore and macropore specific surface area and more mesopore and strong acid center quantity, has excellent iron pollution resistance in application, and can reduce the generation of low value-added products such as dry gas, coke and the like, thereby improving the economic benefit of oil refining.
The specific implementation mode is as follows:
the present invention will be further described with reference to the following examples, which are intended to illustrate only some of the embodiments of the present invention and are not intended to limit the scope of the present invention.
The specification of the raw materials used in the embodiment of the invention is as follows:
kaolin: technical grade, china kaolin ltd, 25.5% scorch;
aluminum sol: self-produced Al 2 O 3 The content was 21.5 wt%;
polyethylene glycol: analytically pure, molecular weight 1000-;
pseudo-boehmite: industrial grade, Shandong division of aluminum, Inc., Shandong province, China, 29.5 wt% burned;
REY molecular sieve: self-production, RE 2 O 3 The content is 7.5-9.0 wt%, and the scorch weight is 25.0 wt%;
phosphorus-aluminum glue: self-made, P 2 O 5 +Al 2 O 3 The content is 40 wt%;
hydrochloric acid: analyzing and purifying;
zinc hydroxide: and (5) analyzing and purifying.
Example 1
(1) Weighing 700 g of kaolin and 160 g of phosphorus-aluminum adhesive (the phosphorus-aluminum ratio is 4.5), adding 600 g of water, controlling the solid content of the slurry to be more than or equal to 50%, mixing and pulping for 16 hours, and controlling the temperature of the slurry to be between 80 and 90 ℃;
(2) weighing 200 g of alumina sol and 0.007 g of polyethylene glycol, adding the polyethylene glycol into the alumina sol, and uniformly stirring for later use;
(3) weighing 360 g of pseudo-boehmite, adding 350 g of water, pulping, and adding 0.5 g of boric acid;
(4)600 g of REY molecular sieve is added with 600 g of water and pulped for standby;
(5) and (3) adding the serous fluid of (1), (2), (3) and (4) into the mixture in a cocurrent flow manner, mixing and pulping, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, performing spray drying, adding 3 g of zinc hydroxide during roasting, washing and drying, and marking a sample as Cat-1.
Example 2
(1) Weighing 700 g of kaolin and 200 g of phosphorus-aluminum adhesive (the phosphorus-aluminum ratio is 4.5), adding 550 g of water, controlling the solid content of the slurry to be more than or equal to 50%, mixing and pulping for 16 hours, and controlling the temperature of the slurry to be between 80 and 90 ℃;
(2) weighing 200 g of alumina sol and 0.007 g of polyethylene glycol, adding the polyethylene glycol into the alumina sol, and uniformly stirring for later use;
(3) weighing 360 g of pseudo-boehmite, adding 350 g of water, pulping, and adding 0.5 g of boric acid;
(4)600 g of REY molecular sieve is added with 600 g of water and pulped for standby;
(5) and (3) adding the serous fluid of (1), (2), (3) and (4) into the mixture in a cocurrent flow manner, mixing and pulping, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, performing spray drying, adding 3 g of zinc hydroxide during roasting, washing and drying, and marking a sample as Cat-2.
Example 3
(1) Weighing 700 g of kaolin and 250 g of phosphorus-aluminum adhesive (the phosphorus-aluminum ratio is 4.5), adding 500 g of water, controlling the solid content of the slurry to be more than or equal to 50%, mixing and pulping for 16 hours, and controlling the temperature of the slurry to be between 80 and 90 ℃;
(2) weighing 200 g of alumina sol and 0.007 g of polyethylene glycol, adding the polyethylene glycol into the alumina sol, and uniformly stirring for later use;
(3) weighing 360 g of pseudo-boehmite, adding 350 g of water, pulping, and adding 0.5 g of boric acid;
(4)600 grams of REY molecular sieve is added with 600 grams of water and beaten for standby;
(5) and (3) adding the serous fluid of (1), (2), (3) and (4) into the mixture in a cocurrent flow manner, mixing and pulping, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, performing spray drying, adding 5 g of zinc hydroxide during roasting, washing and drying, and marking a sample as Cat-3.
Example 4
(1) Weighing 700 g of kaolin and 160 g of phosphorus-aluminum adhesive (the phosphorus-aluminum ratio is 6.0), adding 500 g of water, controlling the solid content of the slurry to be more than or equal to 50%, mixing and pulping for 16 hours, and controlling the temperature of the slurry to be between 80 and 90 ℃;
(2) weighing 200 g of aluminum sol and 0.007 g of polyethylene glycol, adding the polyethylene glycol into the aluminum sol, and uniformly stirring for later use;
(3) weighing 360 g of pseudo-boehmite, adding 350 g of water, pulping, and adding 0.8 g of boric acid;
(4)600 g of REY molecular sieve is added with 600 g of water and pulped for standby;
(5) and (3) adding the serosity of (1), (2), (3) and (4) into the mixture in a parallel flow manner for mixing and pulping, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, performing spray drying, adding 3 g of zinc hydroxide during roasting, washing and drying, and marking a sample as Cat-4.
Example 5
(1) Weighing 700 g of kaolin and 250 g of phosphorus-aluminum adhesive (the phosphorus-aluminum ratio is 6.0), adding 500 g of water, controlling the solid content of the slurry to be more than or equal to 50%, mixing and pulping for 16 hours, and controlling the temperature of the slurry to be between 80 and 90 ℃;
(2) weighing 200 g of alumina sol and 0.007 g of polyethylene glycol, adding the polyethylene glycol into the alumina sol, and uniformly stirring for later use;
(3) weighing 360 g of pseudo-boehmite, adding 350 g of water, pulping, and adding 0.5 g of boric acid;
(4)600 grams of REY molecular sieve is added with 600 grams of water and beaten for standby;
(5) and (3) adding the serous fluid of (1), (2), (3) and (4) into the mixture in a cocurrent flow manner, mixing and pulping, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, performing spray drying, adding 5 g of zinc hydroxide during roasting, washing and drying, and marking a sample as Cat-5.
Comparative example
(1) Weighing 840 g of kaolin and 200 g of alumina sol, adding 1600 g of water, mixing and pulping for 16 hours;
(2) weighing 600 g of REY molecular sieve, adding 1000 g of water, and pulping for later use;
(3) weighing 360 g of pseudo-boehmite;
(4) adding the molecular sieve slurry obtained in the step (2) into the slurry obtained in the step (1) for mixing and pulping, pouring the pseudoboehmite weighed in the step (3) into the mixed slurry for uniformly stirring, supplementing water, keeping the solid content at about 35%, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, and performing spray granulation, washing and drying to obtain a sample labeled as Cat-DB.
The results of the analysis and test of the physicochemical indexes of the catalyst prepared above are shown in table 1:
TABLE 1 catalyst physicochemical data
Figure BDA0003651183430000061
As can be seen from Table 1, the specific surface area of the catalyst prepared by the method is 20-40m higher than that of the normal catalyst 2 G, and this is mainly a result of the increase in the specific surface of the substrate, the variation in the specific surface of the micropores is small.
Adopting an iron naphthenate saturated impregnation method to carry out organic iron pollution impregnation on the catalyst, wherein the target iron amount is 12000ppm, carrying out hydrothermal aging inactivation treatment on the impregnated sample by using a hanging basket hydrothermal aging device, and carrying out aging treatment for 10 hours under the hydrothermal aging condition of 760 ℃ and 100% of water vapor. Finally, the treated catalyst samples are respectively placed in ACE-AP for performance evaluation, the loading amount of the catalyst is 9 g, the reaction temperature is 527 ℃, and the catalyst-oil ratio is 6. The composition of the raw material oil used for evaluation is shown in Table 2, and the ACE evaluation results are shown in Table 3.
TABLE 2 basic Properties of the stock oils
Figure BDA0003651183430000071
TABLE 3 evaluation results of catalysts
Figure BDA0003651183430000072
As can be seen from the evaluation results in Table 3, the catalysts of examples 1-5 have conversion rates significantly higher than those of comparative examples 0.4-1.3 percentage points, and show better iron pollution resistance and excellent product selectivity.

Claims (6)

1. A preparation method of an iron pollution resistant catalytic cracking catalyst comprises the following specific steps:
(1) mixing kaolin and phosphorus-aluminum glue, pulping, controlling the solid content to be more than or equal to 50%, and stirring for more than or equal to 6 hours;
(2) adding polyethylene glycol into the alumina sol, and uniformly stirring for later use;
(3) adding water into pseudo-boehmite for pulping, and adding boric acid for pre-acidification;
(4) adding water into REY molecular sieve, pulping, and stirring uniformly for later use;
(5) and (3) adding the slurry in the steps (1), (2), (3) and (4) into a pulping barrel in a cocurrent flow manner, uniformly stirring, adding hydrochloric acid for acidification, controlling the pH value to be 2.2-3.0, and finally performing spray granulation, roasting, washing and drying to obtain a finished product.
2. The method of claim 1, wherein: in the step (1), the adding proportion of the phosphor-aluminum glue is P 2 O 5 Accounting for 5-10 wt% of the dry basis of the finished product.
3. The system of claim 1The preparation method is characterized by comprising the following steps: in the step (1), the composition of the phosphor-aluminum paste is P 2 O 5 With Al 2 O 3 The molar ratio is 4.5-10.
4. The method of claim 1, wherein: the molecular weight of the polyethylene glycol in the step (2) is 1000-2000g/mol, and the adding proportion accounts for Al 2 O 3 0.001 to 0.01 wt% of the aluminum sol.
5. The method of claim 1, wherein: the adding proportion of the boric acid in the step (3) is H 3 BO 3 Calculated as Al 2 O 3 0.1-0.3 wt% of pseudoboehmite.
6. The method of claim 1, wherein: in the step (5), an opening is added on a pipeline which is connected with the roasting furnace at the bottom of the spraying tower so as to realize the purpose of continuously adding zinc hydroxide, wherein the adding proportion of the zinc hydroxide is 0.1-0.5 wt% of the dry basis of the finished product calculated by ZnO.
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Cited By (2)

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CN116212940A (en) * 2023-03-06 2023-06-06 青岛惠城环保科技集团股份有限公司 Preparation method of catalytic cracking catalyst with excellent coke and dry gas selectivity
CN116212940B (en) * 2023-03-06 2024-06-07 青岛惠城环保科技集团股份有限公司 Preparation method of catalytic cracking catalyst with excellent coke and dry gas selectivity

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