CN107282095B - Catalyst for acrylonitrile production - Google Patents
Catalyst for acrylonitrile production Download PDFInfo
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- CN107282095B CN107282095B CN201610227760.5A CN201610227760A CN107282095B CN 107282095 B CN107282095 B CN 107282095B CN 201610227760 A CN201610227760 A CN 201610227760A CN 107282095 B CN107282095 B CN 107282095B
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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
- B01J29/40—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
- B01J29/48—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 containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
- C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
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- 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 catalyst for acrylonitrile production, which mainly solves the problems of low selectivity and poor stability of a catalyst for propylene ammoxidation in the prior art. The catalyst for producing acrylonitrile comprises a carrier and an active component containing the following general formula: a. theaBbCcNidFeeBifMo13.6OxWherein A is selected from at least one of K, Rb and Cs; b is at least one selected from Ca, Mn, Co, Mg, Cr, W, P and Nb; c is at least one of rare earth elements; the carrier comprises silicon dioxide and a carrier modifier, and the carrier modifier is at least one of aluminum oxide and a ZSM-5 molecular sieve, so that the problem is solved well, and the method can be used in the industrial production of acrylonitrile by propylene ammoxidation.
Description
Technical Field
The present invention relates to a catalyst for acrylonitrile production.
Background
At present, the industrial production of preparing unsaturated nitrile by olefin ammoxidation still generally adopts a fluidized bed ammoxidation process, and a catalyst is taken as one of core technologies of the process, and the research and the improvement of the process are always paid attention. At present, the catalyst for preparing acrylonitrile by industrial propylene ammoxidation mainly comprises two types: Mo-Bi and Sb, wherein Mo-Bi catalysts dominate, reaching 95% of olefin oxidation markets, and the previous research and exploration mainly focuses on Mo-Bi catalysts. The oxidation-reduction performance of the catalyst is improved by introducing metal components with variable valence states, such as Fe, Ce and other elements, into the catalyst, and the recovery of the effective state of the active components of the catalyst is accelerated; by introducing metal elements with the ionic radius of more than 0.8nm and less than 0.8nm, such as Cr, Ni, Mg, Mn, Zn, Al and other elements, the catalyst plays a role of structure and electronic assistant, and improves the structure and stability of the catalyst; by introducing rare earth elements, the amount of lattice oxygen of the catalyst is increased, and the catalytic performance of the catalyst is improved; by introducing elements such as Cs, Rb, P, B, Al and the like, the surface modification and the adjustment of the acidity and alkalinity are carried out on the catalyst, and the selectivity and the activity of the catalyst are improved.
The Mo-Bi series catalysts proposed by patents CN1210033A, CN1285238A, CN1294942A and CN1751790A are suitable for being used under the conditions of higher reaction pressure and high propylene load, and can still keep the characteristic of high single yield of acrylonitrile.
Patents CN03151170.8 and CN03151169.4 describe that in the preparation process of catalyst, solid silica with particle size of 5-100 nm is added in 2-25% of silica sol as carrier starting material to improve the performance of catalyst.
In all of the above patent documents, the oxide catalyst is supported on a silica carrier, and in such oxidation catalyst preparation methods, silica sol is used as a source of silica, however, the influencing factor of silica sol is not mentioned in the above patent documents.
Patent CN1129408A proposes that the aluminum content of the silica sol added during the catalyst preparation process is specified, which can significantly improve the selectivity of acrylonitrile, but there is no clear specification on the content of other components.
Patent CN1744949A proposes to control the pore size distribution of the catalyst by changing the primary particle size of the silica raw material.
Catalysts used for ammoxidation of unsaturated olefins generally include an oxide catalyst comprising oxides of molybdenum, bismuth, iron and at least one element selected from the group consisting of potassium, rubidium and cesium, and a silica carrier having the oxide catalyst supported thereon. Through further research, the additive in the carrier is found to have obvious influence on the selectivity and stability of the propylene ammoxidation reaction.
Disclosure of Invention
The invention aims to solve the technical problems that in the prior art, a catalyst for preparing acrylonitrile by propylene ammoxidation has low selectivity and poor stability, and provides the catalyst for preparing acrylonitrile by propylene ammoxidation, which has the characteristics of high selectivity and good stability.
The second technical problem to be solved by the present invention is to provide a method for preparing the catalyst described in the first technical problem.
The invention also provides a method for producing acrylonitrile by propylene ammoxidation by using the catalyst.
In order to solve one of the above technical problems, the technical scheme adopted by the invention is as follows:
a catalyst for acrylonitrile production, comprising a carrier and an active component containing a compound represented by the general formula: a. theaBbCcNidFeeBifMo13.6Ox
Wherein A is selected from at least one of K, Rb and Cs; b is at least one selected from Ca, Mn, Co, Mg, Cr, W, P and Nb; c is at least one of rare earth elements; the value range of a is 0.01-2.5; the value range of b is 1-15; the value range of c is 0.01-5; d ranges from 1 to 20; the value range of e is 1-15; the value range of f is 0.01-3; x is the total number of oxygen atoms required to satisfy the valence of each element in the catalyst;
the carrier comprises silicon dioxide and a carrier modifier, and the carrier modifier is at least one selected from aluminum oxide and ZSM-5 molecular sieve.
In the technical scheme, the carrier modifier simultaneously comprises a ZSM-5 molecular sieve and alumina, and the two have synergistic effect on the aspects of improving selectivity and stability. The weight ratio of the alumina and the ZSM-5 molecular sieve is not particularly limited, such as, but not limited to, 1: 1 to 10, and more preferably 1: 1 to 5.
In the above technical scheme, the mole ratio of Si/Al in the ZSM-5 molecular sieve is not particularly limited, for example, but not limited to, 20 to 100, and in the specific embodiment of the present invention, the mole ratio of Si/Al is 40 for the same ratio. In the technical scheme of the invention, the ZSM-5 molecular sieve can be selected from a hydrogen type or a sodium type, and in the specific embodiment of the invention, the sodium type ZSM-5 molecular sieve is adopted for comparison.
In the above technical solution, the silica is preferably derived from silica sol.
In the above technical scheme, the amount of the carrier is not particularly limited, and is preferably 30 to 70wt% of the weight of the catalyst.
In the technical scheme, the content of the carrier modifier in the carrier is preferably 0.1-5 wt%.
To solve the second technical problem, the invention adopts the following technical scheme: the preparation method of the catalyst in one of the above technical problems comprises the following steps:
(a) dissolving at least one salt of the corresponding active component elements except Mo in required amount to obtain a solution I;
(b) mixing silica sol with required amount with a carrier modifier to obtain a mixed solution II;
(c) dissolving molybdenum containing molybdate of a required amount, and mixing the molybdenum containing molybdate with the mixed solution II to obtain mixed solution III;
(d) mixing the solution I and the mixed solution III, and stirring at the pH of 1-7 and the temperature of 20-90 ℃ to obtain slurry I;
(e) and (3) carrying out spray drying and roasting and activating on the slurry I at the temperature of 520-660 ℃ for 0.2-4 hours to obtain the required catalyst.
In the above technical solutions, those skilled in the art can understand that, in the step (b), in order to obtain the uniformly dispersed mixed solution II, the carrier modifier is mixed with the silica sol in the form of fine particles, but the particle size of the carrier modifier particles is not particularly limited, and all the particles can obtain comparable inventive effects. Thus, the effect contemplated by the present invention can be obtained as to whether the silica sol is mixed in the form of a sol of the support modifier or a silica sol is mixed with a powder of the support modifier. When silica sol is mixed with the carrier modifier powder, for example, but not limited to, the particle size of the added carrier modifier powder is 10-200 nm, preferably 10-100 nm, and for the purpose of achieving the same ratio between the examples and the comparative examples, in the specific embodiment of the present invention, the particle size of the carrier modifier is 20 nm.
In the technical scheme, the pH value in the step (d) is preferably 1-5.
In the technical scheme, the temperature of the step (d) is preferably 50-80 ℃.
In the technical scheme, the roasting activation temperature is preferably 550-640 ℃.
In the technical scheme, the roasting activation time is preferably 0.5-2 h.
In order to solve the third technical problem, the technical scheme adopted by the invention is as follows: a process for preparing acrylonitrile by ammoxidizing propylene with ammonia features that under the existance of catalyst, the raw materials of propylene, ammonia and air are reacted to obtain acrylonitrile.
In the above technical solutions, those skilled in the art can reasonably determine the reaction process conditions without creative efforts in light of the present inventive concept.
For example, but not limited to, the reaction process is:
1. raw material molar ratio propylene/ammonia/air 1: 1.05-1.3: 9.2 to 9.8.
2. The reaction temperature is 420-440 ℃.
3. The reaction pressure is 0.06-0.14 MPa.
4. The propylene load WWH of the catalyst is 0.06-0.10 h-1。
The technical key point of the invention is that the selectivity and stability of the catalyst to acrylonitrile are improved by including the carrier modifier in the carrier. The evaluation of the activity of the catalyst according to the invention is carried out in a fluidized-bed reactor having an internal diameter of 38 mm. 400 g of catalyst loading, a reaction temperature of 430 ℃, a molar ratio of air to propylene of 9.7:1, a reaction pressure of 0.085Mpa and a reaction load of 0.06 hours-1The operation is carried out for 1000 hours under the condition, the one-way yield of the acrylonitrile reaches about 83 percent, and a better effect is obtained.
The propylene conversion, acrylonitrile selectivity and once-through yield are defined in the present invention as follows:
the invention is further illustrated by the following examples:
Detailed Description
Comparative example 1
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding 2500 g of silica sol with the weight concentration of 40% to obtain a mixed solution II, mixing the solution I and the mixed solution II, and stirring at the temperature of 80 ℃ under the conditions of pH 5 to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Comparative example 2
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2487 g of 40% silica sol, 8 g of water and 5 g of alumina were mixed to form a mixture II, wherein the weight concentration of the carrier in the mixture II was 40% and the carrier contained 0.5 wt% of alumina. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Comparative example 3
Mixing 111.1 g of Bi(NO3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (0)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40% silica sol, 45 g of water and 30 g of alumina are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40%, and the carrier contains 3 wt% of alumina. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Comparative example 4
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2400 g of 40% silica sol, 60 g of water and 40 g of alumina were mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II was 40%, and the carrier contained 4 wt% of alumina. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to micropellet formation in a spray dryer and finally calcined in a rotary kiln at 590 deg.CAnd firing for 2.0 hours to obtain the required catalyst.
Comparative example 5
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2487 g of 40% silica sol, 8 g of water and 5 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the mixed solution II contains 40% of carrier by weight and 0.5 wt% of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Comparative example 6
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40 percent silica sol, 45 g of water and 30 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 3 weight percent of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III,stirring at 80 ℃ and pH 5 to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Comparative example 7
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2400 g of 40 percent silica sol, 60 g of water and 40 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of a carrier in the mixed solution II is 40 percent, and the carrier contains 4 weight percent of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 1
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40 percent silica sol, 45 g of water, 10 g of alumina and 20 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 1 weight percent of alumina and 2 weight percent of ZSM-5And (5) screening by using a secondary screen. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 2
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40 percent silica sol, 45 g of water, 15 g of alumina and 15 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 1.5 percent by weight of alumina and 1.5 percent by weight of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 3
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2O is 160 g of waterHeating and dissolving to obtain solution I. 2425 g of 40 percent silica sol, 45 g of water, 7.5 g of alumina and 22.5 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 0.75 weight percent of alumina and 22.5 weight percent of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 4
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40 percent silica sol, 45 g of water, 6 g of alumina and 24 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 0.6 weight percent of alumina and 2.4 weight percent of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 5
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O、287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2425 g of 40 percent silica sol, 45 g of water, 5 g of alumina and 25 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40 percent, and the carrier contains 0.5 percent by weight of alumina and 2.5 percent by weight of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 6
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2487 g of 40% silica sol, 8 g of water, 1.7 g of alumina and 3.3 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40%, and the carrier contains 0.17 wt% of alumina and 0.33 wt% of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The prepared slurry is formed into microspheres in a spray dryer, and finally is roasted for 2.0 hours in a rotary roasting furnace at 590 ℃ to prepare the required catalyst。
Example 7
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2450 g of 40% silica sol, 30 g of water, 6.7 g of alumina and 13.3 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of the carrier in the mixed solution II is 40%, and the carrier contains 0.67 wt% of alumina and 1.33 wt% of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, adding the mixed solution II to form a mixed solution III, mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
Example 8
111.1 g of Bi (NO)3)3·5H2O, 124.8 g Mn (NO)3)2517.6 g of Ni (NO)3)2·6H2O, 287.6 g Fe (NO)3)3·9H2O, 135.5 g Mg (NO)3)2·6H2O, 3.6 g KOH, 60.7 g Pr (NO)3)3·6H2O and 21.4 g Cr (NO)3)3·9H2The solution I is obtained after the O is dissolved in 160 g of water by heating. 2400 g of 40 percent silica sol, 60 g of water, 13.3 g of alumina and 26.7 g of ZSM-5 molecular sieve are mixed to form a mixed solution II, wherein the weight concentration of a carrier in the mixed solution II is 40 percent, and the carrier contains 1.33 weight percent of alumina and 2.67 weight percent of ZSM-5 molecular sieve. 846.0 g (NH)4)6Mo7O24·4H2Dissolving O in 890 g of water, and adding mixed solution II to form a mixtureAnd mixing the solution I and the mixed solution III, and stirring at the pH of 5 and the temperature of 80 ℃ to obtain slurry I. The resulting slurry was subjected to microsphere formation in a spray dryer and finally calcined in a rotary calciner at 590 ℃ for 2.0 hours to produce the desired catalyst.
The catalysts obtained in examples 1 to 8 and comparative examples 1 to 7 were used for the ammoxidation of propylene to acrylonitrile under the following reaction conditions, and the results are shown in Table 1.
The reaction conditions of the above examples and comparative examples were:
phi 38 mm fluidized bed reactor
The reaction temperature is 435 DEG C
The reaction pressure is 0.085MPa
Catalyst loading 400 g
Catalyst propylene load (WWH) 0.06 hours-1
Raw material ratio (mol) C3 ＝/NH31/1.25/9.7
TABLE 1 catalyst composition and evaluation results
Claims (12)
1. A catalyst for acrylonitrile production, comprising a carrier and an active component containing a compound represented by the general formula: a. theaBbCcNidFeeBifMo13.6Ox
In the formula, A is selected from at least one of K, Rb and Cs, B is selected from at least one of Ca, Mn, Co, Mg, Cr, W, P and Nb, C is selected from at least one of rare earth elements, the value range of a is 0.01-2.5, the value range of B is 1-15, the value range of C is 0.01-5, the value range of d is 1 ~ 20, the value range of e is 1 ~ 15, the value range of f is 0.01-3, and x is the total number of oxygen atoms required by the valence of each element in the catalyst;
the carrier comprises silicon dioxide and a carrier modifier, wherein the carrier modifier is alumina and a ZSM-5 molecular sieve, and the content of the carrier modifier in the carrier is 0.1 ~ 5 wt%.
2. The catalyst of claim 1 wherein the support is present in an amount of 30 ~ 70wt% based on the weight of the catalyst.
3. A method of preparing the catalyst of claim 1, comprising the steps of:
(a) dissolving at least one salt of the corresponding active component elements except Mo in required amount to obtain a solution I;
(b) mixing silica sol with required amount with a carrier modifier to obtain a mixed solution II;
(c) dissolving molybdenum containing molybdate of a required amount, and mixing the molybdenum containing molybdate with the mixed solution II to obtain mixed solution III;
(d) mixing the solution I and the mixed solution III, and stirring at the pH of 1-7 and the temperature of 20-90 ℃ to obtain slurry I;
(e) and (3) spray-drying the slurry I, and roasting and activating the slurry I at 520-660 ℃ for 0.2 ~ 4 h to obtain the required catalyst.
4. The method for preparing a catalyst according to claim 3, wherein the pH in the step (d) is 1 to 5.
5. The method for preparing a catalyst according to claim 3, wherein the temperature in the step (d) is 50 to 80 ℃.
6. The method for preparing a catalyst according to claim 3, wherein the calcination activation temperature is 550 to 640 ℃.
7. The method for preparing the catalyst according to claim 3, wherein the calcination activation time is 0.5 to 2 hours.
8. A process for producing acrylonitrile by ammoxidation of propylene, which comprises reacting propylene, ammonia and air as the raw materials in the presence of the catalyst according to claim 1 or 2 to obtain acrylonitrile.
9. The process according to claim 8, characterized in that the starting material molar ratio of the reaction is propylene/ammonia/air = 1: 1.05-1.3: 9.2 to 9.8.
10. The method according to claim 8, wherein the reaction is carried out at 420-440 ℃.
11. The method according to claim 8, wherein the reaction pressure of the reaction is 0.06-0.14 MPa.
12. The process according to claim 8, characterized in that the catalyst has a propylene load WWH =0.06 ~ 0.10h-1。
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4801727A (en) * | 1987-04-20 | 1989-01-31 | The Standard Oil Company | Method for ammoxidation of paraffins and catalyst system therefor |
| CN1121321A (en) * | 1993-08-10 | 1996-04-24 | 旭化成工业株式会社 | Ammoxidation catalyst composition and process for producing acrylonitrile or methacrylonitrile by using the same |
| CN1346702A (en) * | 2000-09-28 | 2002-05-01 | 罗姆和哈斯公司 | Cocatalytic polymetallic oxide catalyst |
| CN1736592A (en) * | 2005-06-03 | 2006-02-22 | 营口市向阳催化剂有限责任公司 | Fluidized-bed catalyst for ammoxidation of propylene or isobutylene |
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- 2016-04-13 CN CN201610227760.5A patent/CN107282095B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4801727A (en) * | 1987-04-20 | 1989-01-31 | The Standard Oil Company | Method for ammoxidation of paraffins and catalyst system therefor |
| CN1121321A (en) * | 1993-08-10 | 1996-04-24 | 旭化成工业株式会社 | Ammoxidation catalyst composition and process for producing acrylonitrile or methacrylonitrile by using the same |
| CN1346702A (en) * | 2000-09-28 | 2002-05-01 | 罗姆和哈斯公司 | Cocatalytic polymetallic oxide catalyst |
| CN1736592A (en) * | 2005-06-03 | 2006-02-22 | 营口市向阳催化剂有限责任公司 | Fluidized-bed catalyst for ammoxidation of propylene or isobutylene |
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