(19)
(11)EP 3 222 347 B1

(12)EUROPEAN PATENT SPECIFICATION

(45)Mention of the grant of the patent:
20.01.2021 Bulletin 2021/03

(21)Application number: 16873276.6

(22)Date of filing:  30.11.2016
(51)Int. Cl.: 
B01J 23/70  (2006.01)
B01J 21/02  (2006.01)
B01J 29/06  (2006.01)
B01J 37/02  (2006.01)
B01J 23/78  (2006.01)
B01J 23/26  (2006.01)
B01J 37/00  (2006.01)
B01J 35/04  (2006.01)
(86)International application number:
PCT/KR2016/013919
(87)International publication number:
WO 2017/099411 (15.06.2017 Gazette  2017/24)

(54)

CATALYST FOR OXIDATIVE DEHYDROGENATION REACTION AND METHOD FOR PRODUCING SAME

KATALYSATOR FÜR OXIDATIVE DEHYDRIERUNGSREAKTION UND VERFAHREN ZUR HERSTELLUNG DAVON

CATALYSEUR POUR RÉACTION DE DÉSHYDROGÉNATION PAR OXYDATION ET SON PROCÉDÉ DE PRODUCTION


(84)Designated Contracting States:
AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

(30)Priority: 09.12.2015 KR 20150174676
15.12.2015 KR 20150179406

(43)Date of publication of application:
27.09.2017 Bulletin 2017/39

(73)Proprietor: LG Chem, Ltd.
Seoul 07336 (KR)

(72)Inventors:
  • SUH, Myung Ji
    Daejeon 34122 (KR)
  • MIN, Yoon Jae
    Daejeon 34122 (KR)
  • KO, Dong Hyun
    Daejeon 34122 (KR)
  • CHA, Kyong Yong
    Daejeon 34122 (KR)
  • BAEK, Se Won
    Daejeon 34122 (KR)
  • HAN, Jun Kyu
    Daejeon 34122 (KR)

(74)Representative: Goddar, Heinz J. 
Boehmert & Boehmert Anwaltspartnerschaft mbB Pettenkoferstrasse 22
80336 München
80336 München (DE)


(56)References cited: : 
CN-A- 104 001 533
KR-A- 20120 009 687
US-A- 4 440 874
US-A1- 2003 228 457
US-B2- 8 226 740
CN-B- 102 974 357
KR-B1- 100 847 206
US-A1- 2002 183 407
US-A1- 2014 271 390
  
  • TOLEDO, J. A. ET AL.: 'Oxidative Dehydrogenation of 1-butene over Zn-A1 Ferrites' JOURNAL OF MOLECULAR CATALYSIS A: CHEMICAL vol. 125, no. 1, 01 October 1997, pages 53 - 62, XP055069766 DOI: 10.1016/S1381-1169(97)00052-6
  • GIBSON, MICHAEL A. ET AL.: 'Oxidative Dehydrogenation ofButenes over Magnesium Ferrite Catalyst Deactivation Studies' JOURNAL OF CATALYSIS vol. 41, no. 3, 1976, pages 431 - 439, XP055390134
 
Remarks:
The file contains technical information submitted after the application was filed and not included in this specification
 
Note: Within nine months from the publication of the mention of the grant of the European patent, any person may give notice to the European Patent Office of opposition to the European patent granted. Notice of opposition shall be filed in a written reasoned statement. It shall not be deemed to have been filed until the opposition fee has been paid. (Art. 99(1) European Patent Convention).


Description

[Technical Field]


[CROSS-REFERENCE TO RELATED APPLICATIONS]



[0001] This application claims the priority benefit of Korean Patent Application No. 10-2015-0174676, filed on December 09, 2015, and Korean Patent Application No. 10-2015-0179406, filed on December 15, 2015, in the Korean Intellectual Property Office.

[0002] The present invention relates to a method for oxidative dehydrogenation. More particularly, the present invention relates to a method for oxidative dehydrogenation using a catalyst having a porous structure which may easily control heat generation due to high-temperature and high-pressure reaction conditions and side reaction due to the porous structure and thus exhibits superior product selectivity.

[Background Art]



[0003] Demand for 1,3-butadiene, which is an intermediate in petrochemical products, and the value thereof are gradually increasing throughout the world. To produce such 1,3-butadiene, methods, such as naphtha cracking, direct butene dehydrogenation, and oxidative dehydrogenation of butene, have been used. However, in the case of naphtha cracking, energy consumption is high due to high reaction temperature. In addition, since naphtha cracking is not a process specifically designed for production of 1,3-butadiene production, other basic oils, other than 1,3-butadiene, are disadvantageously produced as surplus products. Meanwhile, direct dehydrogenation of normal-butene is thermodynamically unfavorable. In addition, since direct dehydrogenation of normal-butene is an endothermic reaction, high-temperature and low-pressure conditions are required to produce 1,3-butadiene in a high yield. Accordingly, direct dehydrogenation of normal-butene is not suitable as a commercial process for producing 1,3-butadiene.

[0004] Meanwhile, since, in the case of oxidative dehydrogenation of butene wherein butene reacts with oxygen in the presence of a metal oxide catalyst to generate 1,3-butadiene and water, stable water is generated, oxidative dehydrogenation of butene is thermodynamically advantageous. In addition, since oxidative dehydrogenation of butene is an exothermic reaction unlike direct dehydrogenation of butene, oxidative dehydrogenation of butene may produce 1,3-butadiene in a high yield even at low reaction temperature, compared to direct dehydrogenation of butene. In addition, since oxidative dehydrogenation of butene does not require additional heat supply, oxidative dehydrogenation of butene may be considered an effective production process that produces only 1,3-butadiene and thus satisfies demand for 1,3-butadiene. However, in the case of oxidative dehydrogenation, a high calorific value due to a high-temperature reaction condition affects the activity and durability of a metal oxide catalyst, whereby selectivity for 1,3-butadiene is decreased. In addition, since a calorific value further increases due to side reaction, in which Cox is generated, when a high-temperature reaction condition is applied to facilitate a reaction process system, decrease in the activity and performance of a catalyst is accelerated.

[0005] To address the above problems, various technologies, such as a technology of using zeolite with a porous molecular structure as a support for a catalyst or a technology of coating a surface of a catalyst with zeolite, have been reported. However, since zeolite has very fine pores, relief effect thereof on heat generation is very small. Therefore, a catalyst that may more effectively relieve heat generation due to high-temperature and high-pressure reaction conditions and side reaction urgently needs to be developed.

[Related Art Document]



[0006] [Patent Document] (Patent Document 1) US 5041401A

[0007] CN 104001533 A discloses a foam silicon carbide-based structured catalyst and application in preparation of butadiene.

[0008] US 8,226,740 B2 discloses an inorganic material that has metal nanoparticles that are trapped in a mesostructured matrix.

[0009] US 2014/271390 A1 discloses a ZPGM catalyst systems and methods of making the same.

[0010] US 4,440,874 A discloses a catalyst composition and a method of manufacturing the same.

[0011] US 2003/228457 A1 discloses a ceramic body and a ceramic catalyst body.

[0012] US 2002/183407 A1 discloses a macroporous foam comprising microporous zeolithe or zeotype material and preparation thereof by using polymeric templates having sponge structure.

[Disclosure]


[Technical Problem]



[0013] Therefore, the present invention has been made in view of the above problems, and it is one object of the present invention to provide a method for oxidative dehydrogenation having a catalyst having a porous structure which may easily control heat generation due to high-temperature and high-pressure reaction conditions and side reaction due to the porous structure and thus exhibits superior product selectivity.

[0014] The above and other objects can be accomplished by the present disclosure described below.

[Technical Solution]



[0015] The above problems are solved in accordance with the subject-matter of the independent claims. Preferred embodiments result from the sub-claims.

[0016] In accordance with an aspect of the present invention, the above and other objects can be accomplished by the provision of method for the oxidative dehydrogenation of butene to generate 1,3-butadiene wherein the oxidative dehydrogenation is carried out in the presence of a catalyst, the catalyst comprising a porous aluminum silicate support and a metal oxide having a composition represented by Formula 1 below:

        [Formula 1]     [20] AB2O4

wherein A is one or more selected from the group consisting of divalent cation metals and B is one or more selected from the group consisting of trivalent cation metals, wherein A is one or more selected from the group consisting of Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co, and Fe (II), wherein B is one or more selected from the group consisting of Al, Fe(III), Cr, Ga, In, Ti, La, and Ce, and

wherein the porous aluminum silicate support has a pore distribution of 0.394 to 196.85 pores per cm (1 to 500 ppi (pores per inch)).



[0017] The catalyst for oxidative dehydrogenation is obtainable by a method including: a step of immersing a porous rubber in aluminum silicate to be coated with the aluminum silicate; a step of firing the porous rubber coated with the aluminum silicate; a step of obtaining a porous aluminum silicate support; a step of preparing a co-precipitated slurry including a catalyst slurry, which includes a metal oxide, or a precursor of the metal oxide; a step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry to be coated with the catalyst slurry or the co-precipitated slurry; and a step of firing the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry.

[Advantageous effects]



[0018] As apparent from the above description, the present invention provides a method for oxidative dehydrogenation having a catalyst having a porous structure which may easily control heat generation due to high-temperature and high-pressure reaction conditions and side reaction due to the porous structure and thus exhibits superior product selectivity, and a method of preparing the catalyst.

[Description of Drawings]



[0019] FIG. 1 illustrates actual images of a porous rubber, a porous aluminum silicate support, and a catalyst for oxidative dehydrogenation according to the preparation process of the present invention.

[Best mode]



[0020] Hereinafter, the present invention is described in detail.

[0021] The present inventors have continued research into a method for oxidative dehydrogenation. As a result, the present inventors confirmed that, when a catalyst support is prepared using a porous rubber, heat generation due to high-temperature and high-pressure reaction conditions and side reaction is alleviated and thus high selectivity for a product is maintained, thereby completing the present invention.

[0022] Hereinafter, the method for oxidative dehydrogenation according to the present invention is described in detail.

[0023] The catalyst used in the method for oxidative dehydrogenation includes a porous aluminum silicate support and a metal oxide having a composition represented by Formula 1 below:

        [Formula 1]     AB2O4

wherein A is one or more selected from the group consisting of Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co, and Fe (II), preferably one or more selected from the group consisting of Zn, Mg, Mn and Co, and

B is one or more selected from the group consisting of Al, Fe(III), Cr, Ga, In, Ti, La, and Ce, preferably one or more selected from the group consisting of Al, Fe (III) and Cr.



[0024] The metal oxide having the composition represented by Formula 1 may be, for example, a metal oxide having a spinel structure. The spinel structure may be understood as a structure wherein a unit lattice of a cubic system is composed of 8 divalent cations, 16 trivalent cations, and 32 oxygen ions, the oxygen ions mostly forming a face-centered cubic lattice and the divalent cations (A) and the trivalent cations (B) filling spaces between the oxygen ions.

[0025] The metal oxide may be included in an amount of, for example, 1 to 50 % by weight, 1 to 30 % by weight, 5 to 30 % by weight, 2 to 15 % by weight, or 5 to 15 % by weight based on the catalyst for oxidative dehydrogenation. Within this range, oxidative dehydrogenation is initiated.

[0026] The porous aluminum silicate support may be, for example, a sponge-type support. In this case, heat generation due to high-temperature and high-pressure reaction conditions and side reaction may be easily controlled.

[0027] The aluminum silicate of the porous aluminum silicate support may be, for example, a hydrated aluminum silicate. As another example, the aluminum silicate may be a kaolin-based mineral. Particularly, the aluminum silicate may be one or more selected from the group consisting of kaolinite, dickite, nacrite, halloysite, cordierite, diatomite, and mullite. In this case, since the aluminum silicate cannot be oxidatively dehydrogenated or has very low catalytic activity, the aluminum silicate effectively functions as a physical support that is noncompetitive with a metal oxide of a catalyst.

[0028] The porous aluminum silicate support may have, for example, a pore distribution of 0.394 to 196.85 pores per cm (1 to 500 ppi (pores per inch)), 0.394 to 118.11 pores per cm (1 to 300 ppi), or 0.394 to 39.37 pores per cm (1 to 100 ppi). Within this range, high selectivity for a product during oxidative dehydrogenation may be maintained.

[0029] An average particle diameter of pores of the porous aluminum silicate support may be, for example, 0.2 to 10 mm, 0.5 to 5 mm, 1 to 5 mm, or 0.5 to 3 mm Within this range, adsorption and desorption of gaseous reactants and a product to and from a surface of a catalyst are facilitated, whereby the flow of gas is smoothed.

[0030] The porosity of the porous aluminum silicate support may be, for example, 10 to 99 %, 30 to 98 %, 70 to 99 %, or 70 to 98 % with respect to a total volume of the porous aluminum silicate support. Here, the porosity is calculated from a pore volume measured by a liquid impregnation method. Within this range, since retention of heat generated by exothermic reaction is alleviated, heat generated by the exothermic reaction may be effectively controlled, whereby high selectivity for a product is maintained.

[0031] A pore volume of the porous aluminum silicate support may be, for example, 0.1 to 120 cm3/g, 0.1 to 60 cm3/g, 20 to 60 cm3/g, 0.1 to 45 cm3/g, 5 to 45 cm3/g, or 0.1 to 10 cm3/g. Here, the pore volume is calculated from a pore volume measured by a liquid impregnation method.

[0032] The catalyst for oxidative dehydrogenation may be, for example, a sponge-type catalyst. In this case, heat generation due to high-temperature and high-pressure reaction conditions and side reaction may be easily controlled.

[0033] The catalyst for oxidative dehydrogenation has a pore distribution of 0.394 to 196.85 pores per cm (1 to 500 ppi (pores per inch)), 0.394 to 118.11 pores per cm (1 to 300 ppi), or 0.394 to 39.37 pores per cm (1 to 100 ppi). Within this range, high selectivity for a product may be maintained during oxidative dehydrogenation.

[0034] An average particle diameter of pores of the catalyst for oxidative dehydrogenation may be, for example, 1 to 10 mm, 1 to 5 mm, or 1 to 3 mm. Within this range, high selectivity adsorption and desorption of gaseous reactants and a product to and from a surface of a catalyst are facilitated, whereby the flow of gas is smoothed.

[0035] The porosity of the catalyst for oxidative dehydrogenation may be, for example, 10 to 99 %, 30 to 98 %, 70 to 99 %, or 70 to 98 % with respect to a total volume of the catalyst. Here, the porosity is calculated from a pore volume measured by a liquid impregnation method. Within this range, since retention of heat generated by exothermic reaction is alleviated, heat generated by the exothermic reaction is effectively controlled and thus high product selectivity is maintained.

[0036] A pore volume of the catalyst for oxidative dehydrogenation may be, for example, 0.1 to 120 m3/g, 0.1 to 60 cm3/g, 20 to 60 cm3/g, 0.1 to 45 cm3/g, 5 to 45 cm3/g, or 0.1 to 10 cm3/g. Here, the pore volume may be calculated from a pore volume measured by a liquid impregnation method.

[0037] The oxidative dehydrogenation refers to a reaction wherein olefin is reacted with oxygen in the presence of a metal oxide to generate a conjugated diene and water. In a specific example, the oxidative dehydrogenation reaction may be a reaction wherein butene is reacted with oxygen to generate 1,3-butadiene and water.

[0038] A reactor used for the oxidative dehydrogenation is not specifically limited so long as the reactor is a reactor able to be used in oxidative hydrogenation. For example, the reactor may be a reactor wherein reaction temperature of an installed catalyst layer is constantly maintained, and oxidative dehydrogenation proceeds while reactants continuously pass through a catalyst layer. In a particular example, the reactor may be a tubular reactor, a tank reactor, a fluidized bed reactor, or a fixed bed reactor. Here, the fixed bed reactor may be, for example, a multi-tubular reactor or a plate-type reactor.

[0039] A product of the oxidative dehydrogenation may be , for example, one or more selected from the group consisting of butane, isobutane, 1-butene, trans-2-butene, and cis-2-butene and oxygen. The product may further include nitrogen and steam.

[0040] The amount of the oxygen may be, for example, 0.5 to 5 moles, 0.5 to 3 moles, or 0.6 to 1.5 moles based on 1 mole of the reactants. The amount of the nitrogen may be, for example, 0 to 30 moles, 2 to 25 moles, or 2 to 15 moles based on 1 mole of the reactants, and the amount of the steam may be, for example, 2 to 50 moles, 3 to 30 moles, or 4 to 25 moles based on 1 mole of the reactants. Within this range, superior catalytic activity is exhibited.

[0041] During the oxidative dehydrogenation, a gas hourly space velocity (GHSV) may be, for example, 200 to 30,000, 250 to 25,000, or 250 to 20,000 with respect to the reactants.

[0042] During the oxidative dehydrogenation, a reaction temperature (T) may be, for example, 300 to 500 °C, 320 to 400 °C, or 320 to 380 °C.

[0043] During the oxidative dehydrogenation, a reaction pressure may be, for example, 0 to 10 bar, 0 to 5 bar, or 0 to 3 bar,

[0044] 1,3-butadiene selectivity of the catalyst for oxidative dehydrogenation may be, for example, 80 % or more, 85 to 99.9 %, 85 to 93 %, or 93 to 99.9 %.

[0045] A method of preparing the catalyst for oxidative dehydrogenation includes a step of immersing a porous rubber in aluminum silicate to be coated with the aluminum silicate; a step of firing the porous rubber coated with the aluminum silicate; a step of obtaining a porous aluminum silicate support; a step of preparing a co-precipitated slurry including a catalyst slurry, which includes a metal oxide, or a precursor of the metal oxide; a step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry to be coated with the catalyst slurry or the co-precipitated slurry; and a step of firing the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry.

[0046] The step of immersing the porous rubber in aluminum silicate to be coated with the aluminum silicate may include a step of preparing an aluminum silicate slurry; a step of immersing a porous rubber in the aluminum silicate slurry to be coated with the aluminum silicate slurry; and a step of aerating and drying the aluminum silicate slurry-coated porous rubber.

[0047] The aluminum silicate slurry may be prepared, for example, by diluting aluminum silicate with water.

[0048] A weight ratio of the aluminum silicate : water may be, for example, 10:1 to 1:10, 8:1 to 1:8, or 5:1 to 1:5. Within this range, the porous rubber may be entirely coated with the aluminum silicate.

[0049] The aluminum silicate slurry may include, for example, a binder for increasing viscosity in an amount of 0.01 to 10 % by weight, 0.01 to 8 % by weight, or 0.01 to 5 % by weight. The binder may be, for example, one or more selected from the group consisting of polyvinyl alcohol, starch, carboxymethylcellulose, dextrin, wax emulsion, polyethylene glycol, lignosulfonate, methylcellulose, paraffin, and polyacrylate. In this case, adhesion of aluminum silicate to the porous rubber may be increased.

[0050] The porous rubber may be immersed, for example, during a period during which the aluminum silicate slurry contacts an entire area of the porous rubber. Here, the period may be, without being specifically limited, 0.1 to 30 min, 0.1 to 10 min, or 0.1 to 1 min.

[0051] The aerating refers to blowing a gas into the porous rubber coated with the aluminum silicate slurry such that the aluminum silicate slurry does not block pores of the porous rubber. Here, the gas may be, for example, air, nitrogen, helium, or argon. The pressure and temperature of the gas are not specifically limited so long as the coating effect is maintained.

[0052] The porous rubber coated with the aluminum silicate slurry may be dried, for example, at 80 to 160 °C, 90 to 150 °C, or 100 to 140 °C and for 0.5 to 24 hours, 0.5 to 16 hours, or 0.5 to 3 hours. Within this range, moisture is completely removed.

[0053] Each of the step of immersing the porous rubber in the aluminum silicate slurry to be coated with the aluminum silicate slurry and the step of aerating and drying the aluminum silicate slurry-coated porous rubber may be repeated 1 to 10 times, or 1 to 5 rimes.

[0054] The porous rubber coated with the aluminum silicate may be fired, for example, at 1,000 to 2,000 °C, 1,200 to 1,800 °C, or 1,400 to 1,800 °C for 1 to 10 hours, or 1 to 5 hours. Within this range, alpha alumina is formed inside the porous aluminum silicate support, whereby strength and durability increase.

[0055] The porous rubber may be combusted, for example, at 300 to 800 °C, 350 to 700 °C, or 400 to 660 °C during firing. In this case, the porous rubber does not remain in the porous aluminum silicate support.

[0056] The porous rubber is not specifically limited so long as it may be used as a foam. For example, the porous rubber may be polyurethane. In this case, large pores are easily formed.

[0057] The catalyst slurry may be prepared by, for example, by diluting a metal oxide having a composition represented by Formula 1 below with water:

        [Formula 1]     [71] AB2O4

wherein A may be, for example, one or more selected from the group consisting of divalent cation metals, particularly one or more selected from the group consisting of Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co, and Fe (II), preferably one or more selected from the group consisting of Zn, Mg, Mn and Co, and

B may be, for example, one or more selected from the group consisting of trivalent cation metals, particularly one or more selected from the group consisting of Al, Fe(III), Cr, Ga, In, Ti, La, and Ce, preferably one or more selected from the group consisting of Al, Fe(III) and Cr.



[0058] A weight ratio of the metal oxide : water may be, for example, 10:1 to 1:10, 8:1 to 1:8, or 5:1 to 1:5. Within this range, the porous aluminum silicate support may be entirely coated with the metal oxide.

[0059] The metal oxide, for example, may have a powder form and may be prepared through a coprecipitation step, a filtration step, a drying step, and a firing step. In a particular example, the metal oxide may be prepared through (1) a step of preparing a catalyst precursor solution including divalent and trivalent cation metal precursors; (2) a step of adding the catalyst precursor solution dropwise to an aqueous ammonia solution at 10 to 50 °C (pH 7 to 10); (3) a step of stirring the aqueous ammonia solution, to which the catalyst precursor solution has been added, while maintaining pH of the aqueous ammonia solution such that coprecipitation occurs; (4) a step of vacuum filtering a co-precipitated solution to obtain a co-precipitate; (5) a step of drying the obtained co-precipitate at 60 to 150 °C for 6 to 30 hours; and (6) a step of elevating temperature to 400 to 800 °C at a heating rate of 0.5 to 10 °C/min and then maintaining the elevated temperature for 2 to 16 hours such that firing is performed.

[0060] The metal precursors of the step (1) are not specifically limited so long as they are generally used. For example, the metal precursors may be metal salts including divalent or trivalent cation metal ingredients. In a particular example, the metal precursors may be nitrates, ammonium salts, sulfates, or chlorides of the divalent or trivalent cation metal ingredients. In the step (3), pH may be maintained, for example, by simultaneously adding an additional aqueous ammonia solution dropwise when the aqueous catalyst precursor solution is added dropwise.

[0061] The co-precipitated slurry including the metal oxide precursor may be prepared, for example, by coprecipitating the metal oxide having the composition represented by Formula 1 with a catalyst precursor in the same stoichiometric ratio.

[0062] The co-precipitated slurry may be prepared, for example, through (1') a step of preparing a catalyst precursor solution including divalent and trivalent cation metal precursors; (2') a step of adding the catalyst precursor solution dropwise to an aqueous ammonia solution at 10 to 50 °C (pH 7 to 10) ; (3') a step of stirring the aqueous ammonia solution, to which the catalyst precursor solution has been added dropwise, for 30 minutes to 24 hours while maintaining pH of the aqueous ammonia solution such that coprecipitation occurs; and (4') a step of vacuum filtering a resultant co-precipitated solution to adjust the concentration of a co-precipitated slurry.

[0063] The metal precursors of the step (1') are not specifically limited so long as they are generally used. For example, the metal precursors may be metal salts including a divalent or trivalent cation metal ingredient. In a particular example, the metal precursors may be nitrates, ammonium salts, sulfates, or chlorides of the metal ingredient. The concentration of the catalyst precursor solution may be, for example, 1 to 70 % by weight, 2 to 50 % by weight, or 3 to 30 % by weight. When a co-precipitate is fired within this range, the composition represented by Formula 1 is provided. In the step (3'), pH may be maintained, for example, by simultaneously adding an additional aqueous ammonia solution dropwise when the aqueous catalyst precursor solution is added dropwise. In the step (4'), a concentration ratio by weight of the co-precipitated slurry : the sum of the co-precipitate and water may be, for example, 10:1 to 1:10, 8:1 to 1:8, or 5:1 to 1:5. Within this range, the porous aluminum silicate support is entirely coated with the co-precipitate.

[0064] The co-precipitated slurry may include, for example, a binder for increasing viscosity (binder) in an amount of 0.01 to 10 % by weight, 0.01 to 8 % by weight, or 0.01 to 5 % by weight. The binder may be, for example, one or more selected from the group consisting of polyvinyl alcohol, starch, carboxymethylcellulose, dextrin, wax emulsion, polyethylene glycol, lignosulfonate, methylcellulose, paraffin, and polyacrylate. In this case, adhesion of the co-precipitate to the porous aluminum silicate support may be increased.

[0065] The step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry to be coated with the catalyst slurry or the co-precipitated slurry may include a step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry; and a step of aerating and drying the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry.

[0066] The porous aluminum silicate support may be immersed, for example, during a period during which the catalyst slurry or the co-precipitated slurry contacts an entire area of the porous aluminum silicate support. Here, the period may be, without being specifically limited, 0.1 to 30 min, 0.1 to 10 min, or 0.1 to 1 min.

[0067] The aerating refers to blowing a gas into the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry such that the catalyst slurry or the co-precipitated slurry does not block pores of the porous rubber. Here, the gas may be, for example, air, nitrogen, helium, or argon. The pressure and temperature of the gas are not specifically limited so long as the coating effect is maintained.

[0068] The porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry may be dried, for example, at 80 to 160 °C, 90 to 150 °C, or 100 to 140 °C and for 0.5 to 24 hours, 0.5 to 16 hours, or 0.5 to 3 hours. Within this range, moisture is completely removed.

[0069] Each of the step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry; and the step of aerating and drying the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry

aerate and drying may be repeatedly performed 1 to 10 times or 1 to 5 times.

[0070] The porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry may by fired by any method used to prepare a catalyst for oxidative dehydrogenation without specific limitation. For example, the firing may be performed by elevating temperature up to 400 to 800 °C, or 450 to 750 °C at a heating rate of 0.5 to 10 °C /min, 0.5 to 5 °C/min, or 0.5 to 3 °C/min and then maintaining the elevated temperature for 2 to 16 hours, or 3 to 9 hours.

[0071] Now, the present invention will be described in more detail with reference to the following preferred examples. However, these examples are provided for illustrative purposes only. Those skilled in the art will appreciate that various modifications, additions and substitutions are possible, without departing from the scope and spirit of the invention. Therefore, it is obvious that the modifications, additions and substitutions are within the scope of the present invention.

[Example]


Example 1


<Preparation of porous aluminum silicate support>



[0072] Kaolinite (Al2Si2O5(OH)4) and maltodextrin were mixed in a weight ratio of 1:1, thereby preparing a slurry. A polyurethane foam, as a porous rubber having a pore distribution of 5.91 pores per cm (15 ppi (pores per inch)), was immersed in the slurry to coat the polyurethane foam. Here, aeration was performed such that the pores were not blocked, and then drying was performed at 120 °C for 1 hour or more. The dried polyurethane foam was immersed in the slurry again, and aeration and drying were repeated four times. Subsequently, firing was performed at 1,600 °C for two hours, thereby preparing a porous aluminum silicate support.

<Preparation of metal oxide and catalyst slurry>



[0073] 12 g of zinc chloride (ZnCl2) and 48 g of ferric chloride (FeCl3) were dissolved in distilled water, thereby preparing a metal precursor solution. Here, a mole ratio of metal ingredients included in the metal precursor solution was as follows: Zn : Fe = 1 : 2. The prepared metal precursor solution and an aqueous ammonia solution, which was used to maintain pH 9, were simultaneously added to an aqueous ammonia solution at pH 9 and room temperature dropwise, followed by stirring for 1 hour to be co-precipitated. Subsequently, the co-precipitated solution was vacuum filtered to obtain a co-precipitate. The obtained co-precipitate was dried at 90 °C for 16 hours and then temperature was elevated from 80 °C up to 650 °C at a heating rate of 1 °C/min under an air atmosphere. The elevated temperature was maintained for six hours, thereby preparing a zinc-iron oxide (ZnFe2O4) powder having a spinel structure. The prepared metal oxide powder was pulverized to a size of 250 µm or less. The pulverized metal oxide powder was diluted with water in a weight ratio of 1:1, thereby preparing a catalyst slurry.

<Preparation of catalyst for oxidative dehydrogenation>



[0074] The prepared porous aluminum silicate support was immersed in the prepared catalyst slurry and then aeration was performed. Subsequently, drying was performed at 120 °C for one hour. Subsequently, the dried porous aluminum silicate support was immersed in a catalyst slurry again, and then aeration and drying were repeated three times. An obtained catalyst was dried at 120 °C for 16 hours, and temperature was elevated from 80 °C up to 650 °C at a heating rate of 1 °C/min under an air atmosphere. The elevated temperature was maintained for four hours, thereby preparing a catalyst for oxidative dehydrogenation having a porous structure.

Example 2



[0075] An experiment was carried out in the same manner as in Example 1, except that, when a porous aluminum silicate support was prepared, a polyurethane foam, as a porous rubber having a pore distribution of 3.94 pores per cm (10 ppi (pores per inch)). was used instead of the polyurethane foam as a porous rubber having a pore distribution of 5.91 pores per cm (15 ppi).

Example 3



[0076] An experiment was carried out in the same manner as in Example 1, except that, when a porous aluminum silicate support was prepared, a polyurethane foam, as a porous rubber having a pore distribution of 17.72 pores per cm (45 ppi (pores per inch)). was used instead of the polyurethane foam as a porous rubber having a pore distribution of 5.91 pores per cm (15 ppi).

Example 4



[0077] An experiment was carried out in the same manner as in Example 1, except that, when a metal oxide was prepared, a metal precursor solution was prepared by dissolving 12 g of zinc chloride (ZnCl2) , 42 g of iron nitrate (FeNO3), and 6 g of aluminum chloride (AlCl3) , instead of 12 g of zinc chloride (ZnCl2) and 48 g of ferric chloride (FeCl3), in distilled water. Here, a mole ratio of metal ingredients included in the metal precursor solution was as follows: Zn : Fe : Al = 1 : 1.75 : 0.25.

Example 5



[0078] An experiment was carried out in the same manner as in Example 1, except that, when a metal oxide was prepared, a metal precursor solution was prepared by dissolving 18 g of magnesium nitrate (MgNO3) and 48 g of ferric chloride (FeCl3), instead of 12 g of zinc chloride (ZnCl2) and 48 g of ferric chloride (FeCl3), in distilled water. Here, a mole ratio of metal ingredients included in the metal precursor solution was as follows: Mg : Fe = 1 : 2.

Example 6



[0079] An experiment was carried out in the same manner as in Example 1, except that, when a metal oxide was prepared, a metal precursor solution was prepared by dissolving 18 g of manganese nitrate (MnNO3) and 48 g of ferric chloride (FeCl3), instead of 12 g of zinc chloride (ZnCl2) and 48 g of ferric chloride (FeCl3), in distilled water. Here, a mole ratio of metal ingredients included in the metal precursor solution was as follows: Mn : Fe = 1 : 2.

Example 7



[0080] An experiment was carried out in the same manner as in Example 1, except that a co-precipitated slurry was obtained by vacuum filtering a co-precipitated solution when a metal oxide and a catalyst slurry were prepared, and the prepared porous aluminum silicate support was immersed in the prepared co-precipitated slurry when a catalyst for oxidative dehydrogenation was prepared.

Comparative Example 1



[0081] A metal oxide was prepared in the same manner as in Example 1. That is, a co-precipitate was obtained by vacuum filtering a co-precipitated solution, and the obtained co-precipitate was dried at 90 °C for 16 hours, followed by pulverizing the dried co-precipitate into a powder. This powder was mixed and kneaded with water and maltodextrin, followed by extruding by means of a screw-type rotor. The extruded product was cut to a size of 5 mm and then dried, thereby preparing a catalyst having a cylindrical pellet shape. Temperature was elevated from 8C °C to 650 °C at a heating rate of 1 °C/min under an air atmosphere. The elevated temperature was maintained for six hours to fire the catalyst. As a result, a pellet-shaped catalyst was prepared.

[Test example]



[0082] Butadiene was prepared using the catalyst for oxidative dehydrogenation prepared according to each of Examples 1 to 7 and Comparative Example 1. Results are summarized in Table 1 below.

Butadiene preparation



[0083] A mixture of 1-butene, trans-2-butene, and cis-2-butene and oxygen were used as reactants, and nitrogen and steam were additionally introduced along with the reactants. Here, a metallic tubular fixed-bed reactor was used. A reactant ratio and a gas hourly space velocity (GHSV) were determined based on a butene mixture as summarized in Table 1 below. The metallic tubular fixed-bed reactor was filled with 10 cc of each of the catalysts of the examples and the comparative example, and steam was introduced in a water form thereinto. Here, the steam was vaporized at 150 °C by means of a vaporizer and mixed with the reactants, i.e., the butene mixture and the oxygen, such that the steam was flowed along with the reactants into the reactor. After reaction, a product was analyzed using gas chromatography (GC). The conversion rate (X_butene), selectivity (S_1,3-butadiene, S_COx), and yield of a butene mixture were calculated according to Mathematical Equations 1 to 3 below using results measured by gas chromatography:





[Table 1]
ClassificationExamplesComparative example
12345671
Reaction conditions Car (ppi) 15 10 45 15 15 15 15 -
GHSV (hr-1butene) 250 250 250 250 250 250 250 250
  T (°C) 340 360 340 340 340 340 340 340 340
O2/butene 0.75 0.75 0.75 0.75 0.75 0.75 0.75 0.75
Steam/butene 15 15 15 15 15 15 15 15
N2/butene 3 3 3 3 3 3 3 3
Reaction results X-butene 32.3 49.0 39.9 56.6 34.6 40.0 24.4 49.8 46.11
S-1, 3-butadiene 96.3 94.9 92.8 90.6 89.8 84.8 88.4 95.6 92.24
Yield 31.1 46.5 37.0 51.2 31.1 33.9 21.6 47. 6 42.53
S-CO2 2.2 4.1 6.1 7.5 8.4 11.9 10.1 3.1 6.33


[0084] As shown in Table 1, it can be confirmed that, in the cases of Example 1 to 7 in which the catalyst having a porous structure prepared according to the present invention was used, butene conversion rate, butadiene selectivity, and yield are all superior.

[0085] On the other hand, it can be confirmed that, in the case of Comparative Example 1 in which a pellet-shaped catalyst was used using a metal oxide having the same composition as that of Example 1, butene conversion rate, butadiene selectivity, and yield are all poor, compared to the case of the Example 1.

[Reference example]



[0086] Butadiene of a test example was prepared as follows. The catalyst for oxidative dehydrogenation prepared according to Example 1 was used, and O2, steam, and N2 were injected in a mole ratio of 1:4:12 with respect to 1 mol of butene at a reaction temperature (T) of 360 °C such that reaction occurred. As result, X_butene was 56.56, S_1,3-butadiene was 90.55, a yield was 51.22, and S_COx was 7.46. From these results, it can be confirmed that catalytic activity improves as the ratio of steam to the butene mixture increases.

[0087] From these results, the present inventors confirmed that, when a porous catalyst was prepared using a porous rubber, heat generation due to high-temperature and high-pressure reaction conditions and side reaction is alleviated, whereby high selectivity for a product may be maintained.


Claims

1. Method for the oxidative dehydrogenation of butene to generate 1,3-butadiene wherein the oxidative dehydrogenation is carried out in the presence of a catalyst, the catalyst comprising a porous aluminum silicate support and a metal oxide having a composition represented by Formula 1 below:

        [Formula 1]     AB2O4

wherein A is one or more selected from the group consisting of divalent cation metals and B is one or more selected from the group consisting of trivalent cation metals,

wherein A is one or more selected from the group consisting of Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co, and Fe (II),

wherein B is one or more selected from the group consisting of Al, Fe(III), Cr, Ga, In, Ti, La, and Ce, and

[wherein the porous aluminum silicate support has a pore distribution of 0.394 to 196.85 pores per cm (1 to 500 ppi (pores per inch)).


 
2. The method according to claim 1, wherein the metal oxide is comprised in an amount of 1 to 50 % by weight based on the catalyst for oxidative dehydrogenation.
 
3. A method according to claim 1 wherein the catalyst is obtainable by a preparation comprising the steps of":

a step of immersing a porous rubber in aluminum silicate to be coated with the aluminum silicate;

a step of firing the porous rubber coated with the aluminum silicate;

a step of obtaining a porous aluminum silicate support;

a step of preparing a co-precipitated slurry or a catalyst slurry, which comprises a metal oxide, or a precursor of the metal oxide;

a step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry to be coated with the catalyst slurry or the co-precipitated slurry; and

a step of firing the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry.


 
4. The method according to claim 3, wherein the step of immersing the porous rubber in aluminum silicate to be coated with the aluminum silicate comprises a step of preparing an aluminum silicate slurry; a step of immersing a porous rubber in the aluminum silicate slurry to be coated with the aluminum silicate slurry; and a step of aerating and drying the aluminum silicate slurry-coated porous rubber.
 
5. The method according to claim 3, wherein the porous rubber coated with aluminum silicate is fired at 1,200 to 2,000 °C for 1 to 4 hours.
 
6. The method according to claim 3, wherein the porous rubber is polyurethane.
 
7. The method according to claim 3, wherein the catalyst slurry is prepared by diluting a metal oxide having a composition represented by Formula 1 below with water:

        [Formula 1]      AB2O4

wherein A is one or more selected from the group consisting of divalent cation metals and B is one or more selected from the group consisting of trivalent cation metals.
 
8. The method according to claim 7, wherein a weight ratio of the metal oxide : the water is 10:1 to 1:10.
 
9. The method according to claim 3, wherein the step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry to be coated with the catalyst slurry or the co-precipitated slurry comprises a step of immersing the porous aluminum silicate support in the catalyst slurry or the co-precipitated slurry; and a step of aerating and drying the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry.
 
10. The method according to claim 9, wherein the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry is dried at 80 to 160 °C for 0.5 to 24 hours.
 
11. The method according to claim 3, wherein, to fire the porous aluminum silicate support coated with the catalyst slurry or the co-precipitated slurry, temperature is elevated up to 400 to 800 °C at a heating rate of 0.5 to 10 °C/min and then the elevated temperature is maintained for 2 to 16 hours.
 


Ansprüche

1. Verfahren zur oxidativen Dehydrogenierung von Buten, um 1,3-Butadien zu erzeugen, wobei die oxidative Dehydrogenierung in Gegenwart eines Katalysators durchgeführt wird, wobei der Katalysator einen porösen Aluminiumsilikatträger und ein Metalloxid mit einer Zusammensetzung, die durch die folgende Formel 1 dargestellt ist, umfasst:

        [Formel 1]     AB2O4

wobei A eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus divalenten Kationenmetallen und B eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus trivalenten Kationenmetallen,

wobei A eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co und Fe(II),

wobei B eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus Al, Fe(III), Cr, Ga, In, Ti, La und Ce, und

wobei der poröse Aluminiumsilikatträger eine Porenverteilung von 0,394 bis 196,85 Poren pro cm (1 bis 500 ppi (Poren pro Inch)) hat.


 
2. Verfahren nach Anspruch 1, wobei das Metalloxid in einer Menge von 1 bis 50 Gewichtsteilen, bezogen auf den Katalysator für die oxidative Dehydrogenierung, umfasst ist.
 
3. Verfahren nach Anspruch 1, wobei der Katalysator erhältlich ist durch eine Herstellung, umfassend die Schritte:

einen Schritt des Eintauchens von porösem Kautschuk in Aluminiumsilikat, um von dem Aluminiumsilikat beschichtet zu werden;

einen Schritt des Brennens des porösen Kautschuks, der mit dem Aluminiumsilikat beschichtet ist;

einen Schritt des Erhaltens eines porösen Aluminiumsilikatträgers;

einen Schritt des Herstellens einer co-ausgefällten Aufschlämmung oder einer Katalysatoraufschlämmung, die ein Metalloxid oder einen Vorläufer des Metalloxids umfasst;

einen Schritt des Eintauchens des porösen Aluminumsilikatträgers in die Katalysatoraufschlämmung oder die co-ausgefällten Aufschlämmung, um die Katalysatoraufschlämmung oder co-ausgefällten Aufschlämmung zu beschichten ist; und

einen Schritt des Erhitzens des porösen Aluminiumsilikatträgers, um von der der Katalysatoraufschlämmung oder der co-ausgefällten Aufschlämmung beschichtet zu werden.


 
4. Verfahren nach Anspruch 3, wobei der Schritt des Eintauchens des porösen Kautschuks in Aluminiumsilikat, um mit dem Aluminiumsilikat beschichtet zu werden, einen Schritt des Herstellens einer Aluminiumsilikataufschlämmung; einen Schritt des Eintauchens des porösen Kautschuks in die Aluminiumsilikataufschlämmung, um mit dem Aluminiumsilikat beschichtet zu werden; und einen Schritt des Belüftens und Trocknens des Aluminiumsilikataufschlämmungs-beschichteten porösen Kautschuks umfasst.
 
5. Verfahren nach Anspruch 3, wobei der poröse Kautschuk, der mit dem Aluminiumsilikat beschichtet ist, bei 1.200 bis 2.000°C für 1 bis 4 Stunden erhitzt wird.
 
6. Verfahren nach Anspruch 3, wobei der poröse Kautschuk Polyurethan ist.
 
7. Verfahren nach Anspruch 3, wobei die Katalysatoraufschlämmung durch Verdünnen eines Metalloxids einer Zusammensetzung, die durch die Formel 1 dargestellt ist, mit Wasser hergestellt wird:

        [Formel 1]     AB2O4

wobei A eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus divalenten Kationenmetallen und B eines oder mehrere ist, ausgewählt aus der Gruppe, bestehend aus trivalenten Kationenmetallen.
 
8. Verfahren nach Anspruch 7, wobei ein Gewichtsverhältnis von Metalloxid : Wasser 10:1 bis 1:10.
 
9. Verfahren nach Anspruch 3, wobei der Schritt des Eintauchens des porösen Aluminiumsilikatträgers in die Katalysatoraufschlämmung oder die co-ausgefällten Aufschlämmung, um mit der Katalysatoraufschlämmung oder die co-ausgefällten Aufschlämmung werden, einen Schritt des Eintauchens des porösen Aluminiumsilikatträgers in die Katalysatoraufschlämmung oder der co-ausgefällten Aufschlämmung umfasst; und einen Schritt des Belüftens und Trocknens des porösen Aluminiumsilikatträgers, beschichtet mit der Katalyatoraufschlämmung oder der co-ausgefällten Schlämmung, umfasst.
 
10. Verfahren nach Anspruch 9, wobei der poröse Aluminiumsilikatträger, der mit der Katalysatoraufschlämmung oder der co-ausgefällten Aufschlämmung beschichtet ist, bei 80 bis 160°C für 0,5 bis 24 Stunden getrocknet wird.
 
11. Verfahren nach Anspruch 3, wobei, um den porösen Aluminiumsilikatträger, der mit der Katalysatoraufschlämmung oder der co-ausgefällten Aufschlämmung beschichtet ist, zu brenne, die Temperatur auf 400 bis 8oo°C mit einer Aufheizrate von 0,5 bis 10°C/min erhöht wird und dann die erhöhte Temperatur für 2 bis 16 Stunden beibehalten wird.
 


Revendications

1. Procédé de déshydrogénation oxydative du butène pour générer du 1,3-butadiène, dans lequel la déshydrogénation oxydative est effectuée en présence d'un catalyseur, le catalyseur comprenant un support poreux de silicate d'aluminium et un oxyde métallique ayant une composition représentée par la formule 1 ci-dessous :

        [Formule 1]     AB2O4

dans laquelle formule, A représente un ou plusieurs éléments sélectionnés dans le groupe constitué de métaux cationiques divalents et B représente un ou plusieurs composés sélectionnés dans le groupe constitué de métaux cationiques trivalents,

dans laquelle formule, A représente un ou plusieurs éléments sélectionnés dans le groupe constitué de Cu, Ra, Ba, Sr, Ca, Be, Zn, Mg, Mn, Co et de F2 (II),

dans laquelle formule, B représente un ou plusieurs éléments sélectionnés dans le groupe constitué de Al, F2 (III), Cr, Ga, In, Ti, La et de Ce, et

(dans lequel procédé le support poreux en silicate d'aluminium a une distribution de pores de 0,394 à 196,85 pores par cm (1 à 500 ppi (pores par pouce)).
 
2. Procédé selon la revendication 1, dans lequel l'oxyde métallique est compris en une quantité de 1 à 50 % en poids par rapport au catalyseur de déshydrogénation oxydative.
 
3. Procédé selon la revendication 1, dans lequel le catalyseur peut être obtenu par une préparation comprenant les étapes suivantes :

une étape d'immersion d'un caoutchouc poreux dans du silicate d'aluminium appelé à être revêtu du silicate d'aluminium ;

une étape de cuisson du caoutchouc poreux revêtu du silicate d'aluminium ;

une étape d'obtention d'un support poreux de silicate d'aluminium ;

une étape de préparation d'une suspension coprécipitée ou d'une suspension catalytique, qui comprend un oxyde métallique ou un précurseur de l'oxyde métallique ;

une étape d'immersion du support poreux de silicate d'aluminium dans la suspension catalytique ou la suspension co-précipitée appelée à être revêtue de la suspension catalytique ou de la suspension co-précipitée ; et

une étape de cuisson du support poreux de silicate d'aluminium revêtu de la suspension catalytique ou de la suspension coprécipitée.


 
4. Procédé selon la revendication 3, dans lequel l'étape d'immersion du caoutchouc poreux dans du silicate d'aluminium appelé à être revêtu du silicate d'aluminium comprend une étape de préparation d'une suspension de silicate d'aluminium ; une étape d'immersion d'un caoutchouc poreux dans la suspension de silicate d'aluminium appelée à être revêtue de la suspension de silicate d'aluminium ; et une étape d'aération et de séchage du caoutchouc poreux revêtu de la suspension de silicate d'aluminium.
 
5. Procédé selon la revendication 3, dans lequel le caoutchouc poreux revêtu du silicate d'aluminium est cuit à une température de 1.200 à 2.000 °C pendant 1 à 4 heures.
 
6. Procédé selon la revendication 3, dans lequel le caoutchouc poreux est du polyuréthane.
 
7. Procédé selon la revendication 3, dans lequel la suspension catalytique est préparée en diluant un oxyde métallique ayant une composition représentée par la formule 1 ci-dessous avec de l'eau :

        [Formule 1]     AB2O4

dans laquelle formule, A représente un ou plusieurs éléments sélectionnés dans le groupe constitué de métaux à cations divalents et B représente un ou plusieurs éléments sélectionnés dans le groupe constitué de métaux à cations trivalents.
 
8. Procédé selon la revendication 7, dans lequel le rapport en poids entre l'oxyde métallique et l'eau est de 10 : 1 à 1 : 10.
 
9. Procédé selon la revendication 3, dans lequel l'étape d'immersion du support poreux de silicate d'aluminium dans la suspension catalytique ou la suspension coprécipitée appelée à être revêtue de la suspension catalytique ou de la suspension coprécipitée comprend une étape d'immersion du support poreux de silicate d'aluminium dans la suspension catalytique ou la suspension coprécipitée ; et une étape d'aération et de séchage du support poreux de silicate d'aluminium avec la suspension catalytique ou la suspension coprécipitée.
 
10. Procédé selon la revendication 9, dans lequel le support poreux de silicate d'aluminium revêtu de la suspension catalytique ou de la suspension coprécipitée est séché à une température de 80 à 160 °C pendant 0,5 à 24 heures.
 
11. Procédé selon la revendication 3, dans lequel, pour cuire le support poreux de silicate d'aluminium revêtu de la suspension catalytique ou de la suspension coprécipitée, la température est élevée jusqu'à 400 à 800 °C à une vitesse de chauffage de 0,5 à 10 °C/min et la température élevée est maintenue pendant 2 à 16 heures.
 




Drawing






REFERENCES CITED IN THE DESCRIPTION



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Patent documents cited in the description