Supported Catalyst, Preparation Method Therefor

(19) TZZ¥Z _T

(11) EP 3 056 269 B1

(12) EUROPEAN PATENT SPECIFICATION

(45) Date of publication and mention (51) Int Cl.: of the grant of the patent: B01J 27/138 (2006.01) B01J 37/22 (2006.01) 24.04.2019 Bulletin 2019/17 C07C 11/09 (2006.01) C07C 1/26 (2006.01) B01J 29/40 (2006.01) (21) Application number: 14859617.4 (86) International application number: (22) Date of filing: 28.10.2014 PCT/CN2014/089683

(87) International publication number: WO 2015/067133 (14.05.2015 Gazette 2015/19)

(54) SUPPORTED CATALYST, PREPARATION METHOD THEREFOR AND USE THEREOF, AND METHOD FOR PREPARATION OF ISOBUTYLENE FROM HALOMETHANE GETRÄGERTER KATALYSATOR, HERSTELLUNGSVERFAHREN DAFÜR UND VERWENDUNG DAVON SOWIE VERFAHREN ZUR HERSTELLUNG VON ISOBUTYLEN AUS HALOMETHAN CATALYSEUR SUPPORTÉ, SON PROCÉDÉ DE PRÉPARATION ET SON UTILISATION, ET PROCÉDÉ DE PRÉPARATION D’ISOBUTYLÈNE À PARTIR D’UN HALOMÉTHANE

(84) Designated Contracting States: • ZHANG, Xiwen AL AT BE BG CH CY CZ DE DK EE ES FI FR GB Fushun GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO Liaoning 113001 (CN) PL PT RO RS SE SI SK SM TR • SUN, Xiaodan Fushun (30) Priority: 07.11.2013 CN 201310546339 Liaoning 113001 (CN) • LI, Jie (43) Date of publication of application: Fushun 17.08.2016 Bulletin 2016/33 Liaoning 113001 (CN) • NI, Xiangqian (73) Proprietors: Fushun • China Petroleum & Chemical Corporation Liaoning 113001 (CN) Beijing 100728 (CN) • Fushun Research Institute of Petroleum and (74) Representative: Hoffmann Eitle Petrochemicals, Sinopec Corp. Patent- und Rechtsanwälte PartmbB Fushun, Liaoning 113001 (CN) Arabellastraße 30 81925 München (DE) (72) Inventors: • FANG, Xiangchen (56) References cited: Fushun EP-A1- 1 421 992 CN-A- 1 502 411 Liaoning 113001 (CN) CN-A- 86 107 833 CN-A- 101 342 494 • ZHANG, Shudong US-A- 4 091 038 US-A- 4 154 969 Fushun US-A1- 2009 163 749 Liaoning 113001 (CN) • ZHANG, Xinwei Fushun Liaoning 113001 (CN)

Note: Within nine months of the publication of the mention of the grant of the European patent in the European Patent Bulletin, any person may give notice to the European Patent Office of opposition to that patent, in accordance with the Implementing Regulations. Notice of opposition shall not be deemed to have been filed until the opposition fee has been paid. (Art. 99(1) European Patent Convention). EP 3 056 269 B1

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Description

Field of the Invention

5 [0001] The present invention relates to a supported catalyst, method for its preparation and use thereof, and a method for preparation of isobutylene from halomethane by using this supported catalyst.

Background of the Invention

10 [0002] Isobutylene is an important basic organic chemical raw material. It has numerous derivatives. Its upstream and downstream industrial chains are complex. Its consumption structure is in diversified trends. From isobutylene, many products with high added value may be prepared, such as: butyl rubber, polyisobutylene, methyl tertiary-butyl ether, isoprene, polymethyl methacrylate and many other organic chemical raw materials and fine chemical products. As the market size of isobutylene downstream products keeps expanding, the imbalance between supply and demand will get 15 more prominent. Particularly, under the background of increasing depletion of petroleum resources, the output of isobutylene has become a critical bottleneck holding back the development of downstream industry. Therefore, it is urgent to develop an isobutylene preparation route rather than a petroleum route. [0003] Methane is a main component of natural gas, so methane conversion and utilization becomes an important research content of natural gas chemical technology. Particularly, in the recent years, under the general background of 20 shale gas development and utilization, if isobutylene can be made from methane, it will be a new way to obtain isobutylene. However, methane has stable properties and is not easily activated, so it turns to be a bottleneck of chemical utilization of methane. Many domestic and foreign researchers have carried out the research of methane activation and conversion. The technology of halogen functionalization and then conversion of methane hopefully will become an important break- through to the technical problem of methane conversion. 25 [0004] From halomethane, many chemical products may be prepared. CN101041609A and CN101284232A disclose a method of converting methane into bromomethane under the action of oxygen and HBr/H2O and then taking further reaction of bromomethane to generate C3∼C13 mixed high-carbon hydrocarbons. The selectivity of hydrocarbons of C 5 or higher is 70%. HBr is used to bromize methane in the first reactor and released in the second reactor. After recovery, it is used in the first reaction again to realize cyclic use of HBr. Wang Ye et al (Jieli He, Ting Xu, Zhihui Wang, et.al. 30 Angew.Chem. Int. Ed. 2012, 51,2438-2442) discloses amodified molecular sieve catalystof propylene from halomethane and preparation method thereof. By using a molecular sieve modified and treated with fluorinated compound to obtain an acidic catalyst containing an appropriate micropore structure, this catalyst may effectively catalyze halomethane and convert it into propylene. In the preparation and conversion of propylene from bromomethane, the single-pass bromomethane conversion rate of the prepared catalyst is 35-99% and the selectivity of propylene is 27-70%; in the prep- 35 aration and conversion of propylene from chloromethane, the single-pass chloromethane conversion rate is 30-99% and the selectivity of propylene is 15-70%. Ivan M. Lorkovic et al (Ivan M. Lorkovic, Aysen Yilmaz, Gurkan A. Yilmaz, et al. Catalysis Today, 2004, 98, 317-322) also put forth a bromine circulation of using bromine to react with hydrocarbons in natural gas to generate bromo-hydrocarbons, then converting bromo-hydrocarbons into dimethyl ether, methanol and metal bromide on a metal oxide catalyst, and regenerating metal bromide by oxygen to obtain metal oxide and release 40 simple substance bromine. [0005] At present, the target products of halomethane conversion in the existing literature are methanol, dimethyl ether, acetic acid, high-carbon hydrocarbon, ethylene and propylene. In the technologies in which low-carbon olefins with high added value are target products, the selectivity of a single product is not high. So far there is no report on highly selective synthesis of isobutylene from bromomethane. 45 [0006] US 4,091,038 describes a process for producing dihydroxy diphenyl ethane which comprises reacting phenol with a 1,2-dihaloethane in which the halogen is chlorine, bromine or iodine in at least the stoichiometric proportions of 2/1 in contact with a zinc-containing catalyst at a temperature of from about 125 to 225°C and in the presence of iodine as promoter for the reaction. [0007] US 4,154,969 describes employing a combination of zinc oxide and zinc bromide as catalyst for the reaction 50 between phenol and a 1,2-dihaloethane. [0008] EP 1,421,992 discloses a method for producing a zinc chloride-loaded support in which zinc chloride is loaded on a solid support, comprising a step of bringing a mixture of the solid support and zinc oxide into contact with water vapor containing a hydrogen chloride gas or a hydrogen chloride gas so that said zinc oxide is chemically converted into zinc chloride. 55 [0009] US 2009/0163749 discloses a process for converting methane into higher hydrocarbons comprising contacting methane with a source of oxygen and hydrogen bromide to form one or more methane bromide compounds, in the presence of a first catalyst within a first reactor, converting the methane bromides into C 3-13 hydrocarbons and hydrogen bromide in the presence of a second catalyst within a second reactor.

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Summary of the Invention

[0010] To address the shortcomings of prior art, the present invention provides a supported catalyst for highly selective generation of isobutylene from halomethane and its preparation method and use. 5 [0011] According to one aspect of the present invention, the present invention provides a supported catalyst, wherein the catalyst contains a support and a metallic active component supported on the support; the metallic active component contains zinc oxide and zinc halide, and the content of zinc oxide is 0.5 wt.%-20 wt.%, the content of zinc halide is 10 wt.%-50 wt.%, and the content of the support is 40 wt.%-88 wt.% based on the total weight of the catalyst. [0012] According to the second aspect of the present invention, the present invention provides a method for preparing 10 a supported catalyst, wherein the method includes the steps as defined in the claims. According to the third aspect of the present invention, the present invention provides a use of the supported catalyst of the present invention in preparation of isobutylene. [0013] According to the fourth aspect of the present invention, the present invention provides a method for preparation of isobutylene from halomethane, wherein the method includes carrying out hydrogen reduction activation of the sup- 15 ported catalyst of the present invention to make the content of halogen in the activated catalyst be 20 wt.%-90 wt.% of the total content of halogen in the supported catalyst without reduction, then contacting halomethane with the activated catalyst to prepare isobutylene. Compared with prior art, the catalyst of the present invention may convert halomethane into isobutylene with high selectivity. The reaction for conversion and preparation of isobutylene from bromomethane is conducted by the method of the present invention. The bromomethane conversion rate is 90% or more and the selectivity 20 of isobutylene is 80% or more. The preparation method of this catalyst is simple and can be easily industrialized. The method for preparation and conversion of isobutylene from bromomethane in the present invention has such advantages as moderate reaction conditions and high product selectivity, can be easily industrialized and has a broad application prospect.

25 Detailed Description of the Embodiments

[0014] According to one aspect of the present invention, the present invention provides a supported catalyst, wherein the catalyst contains a support and a metallic active component supported on the support, the metallic active component contains zinc oxide and zinc halide, and the content of zinc oxide is 0.5 wt.%-20 wt.%, the content of zinc halide is 10 30 wt.%-50 wt.%, and the content of the support is 40 wt.%-88 wt.% based on the total weight of the catalyst. [0015] Preferably, based on the total weight of the catalyst, the content of zinc oxide is 1 wt.%-15 wt.%, the content of zinc halide is 15 wt.%-45 wt.%, and the content of the support is 50 wt.%-84 wt.%, more preferably, the content of zinc oxide is 1 wt.%-9 wt.%, the content of zinc halide is 18 wt.%-39 wt.%, and the content of the support is 55 wt.%-80 wt.% based on the total weight of the catalyst. According to the present invention, the zinc halide may be selected from 35 one or more of zinc fluoride, zinc chloride, zinc bromide and zinc iodide. The support may be one or more of aluminum oxide, silicon oxide and ZSM-5 molecular sieve. [0016] Preferably, the zinc halide is zinc bromide, and the support is aluminum oxide. The aluminum oxide may be γ- aluminum oxide and/or 0-aluminum oxide. [0017] According to the supported catalyst of the present invention, preferably, this catalyst further contains an ap- 40 propriate amount of promoter, which is selected from one or more of Ti, Zr, Ce and La. More preferably, the promoter is Zr. [0018] The weight content of the promoter calculated on element is 0.1 wt.%-10 wt.%, more preferably 0.5 wt.%-5 wt.%, still more preferably 0.5 wt.%-3 wt.% based on the total weight of the catalyst.

[0019] According to the supported catalyst of the present invention, it is determined by NH 3-TPD method that the total acidity of 450°C or less in the catalyst is 0.5 mmol/g-1.3 mmol/g, and the acidity of 250°C-350°C is 20%-90% of the total 45 acidity of 450°C or less; preferably, the total acidity of 450°C or less in the catalyst is 0.6 mmol/g-1.2 mmol/g, and the acidity of 250°C-350°C is 30%-80% of the total acidity of 450°C or less; more preferably, the total acidity of 450°C or less in the catalyst is 0.7 mmol-1.1 mmol/g, and the acidity of 250°C-350°C is 40%-80% of the total acidity of 450°C or

less. In the present invention, the acids determined by NH 3-TPD method in correspondence to 150°C-250°C are weak acids, the acids in correspondence to 250°C-400°C are mid-strong acids, and the acids in correspondence to 400°C- 50 500°C are strong acids; the sum of the acid content of weak acids, moderately strong acids and strong acids are total acid content. [0020] According to the method for preparing a supported catalyst in the present invention, wherein the method includes the following steps: introducing zinc oxide to the support and then halogenating the resulted support after introducing zinc oxide, wherein the means of the halogenation includes contacting gaseous-phase halogen-containing compound 55 with the support containing the introduced zinc oxide under the contact conditions that make the zinc oxide on the support partially converted into zinc halide. [0021] The amount of introduced zinc oxide and the conditions of halogenation make the content of zinc oxide be 0.5 wt.%-20 wt.%, the content of zinc halide be 10 wt.%-50 wt.%, and the content of the support be 40 wt.%-88 wt.% based

3 EP 3 056 269 B1

on the total weight of the obtained supported catalyst. Preferably, the content of zinc oxide is 1 wt.%-15 wt.%, the content of zinc halide is 15 wt.%-40 wt.%, and the content of the support is 50 wt.%-84 wt.%, more preferably, the content of zincoxide is 1 wt.%-9wt.%, the contentof zinc halideis 18 wt.%-39wt.%, and the content ofthe supportis 55 wt.%-80wt.%. [0022] According to the present invention, various means may be adopted to halogenate the support containing the 5 introduced zinc oxide as long as an appropriate amount of zinc oxide in it is converted into zinc halide. [0023] Gaseous-phase halogen-containing compound may directly contact the support containing the introduced zinc oxide. Alternatively, gaseous-phase halogen-containing compound may contact the support containing the introduced zinc oxide in a form of a mixed gas of gaseous-phase halogen-containing compound and inert gas. In the mixed gas, the concentration of the gaseous-phase halogen-containing compound is not less than 20 v/v%., preferably not less 10 than 30 v/v%, more preferably 30-90 v/v%, still more preferably 50-80 v/v%. [0024] The gaseous-phase halogen-containing compound may be various kinds of halogen-containing compounds that are gaseous under the contact conditions, preferably halomethane, more preferably one or more of monohalomethane, bihalomethane and trihalomethane, still more preferably monohalomethane. [0025] The halogen may be one or more of F, Cl, Br and I, preferably Cl and/or Br. 15 [0026] More preferably, the gaseous-phase halogen-containing compound is monobromomethane. [0027] According to the present invention, the preferred means of the contact includes putting the support containing the introduced zinc oxide in a continuous flow fixed bed reactor, raising temperature to 150°C-400°C in an inert atmosphere, and inputting gaseous-phase halogen-containing compound or a mixed gas containing gaseous-phase halogen- containing compound. The space velocity is 50h-1-1000 h-1, the contact pressure is 0.1MPa-0.5MPa and the time is 20 0.5h-8h. Preferably, temperature is raised to 180°C-350°C in an inert atmosphere, more preferably, the temperature is raised to 200°C-300°C, the space velocity is 100h -1-500h-1, the contact pressure is 0.1MPa-0.3MPa and the time is 1h- 4h. The pressure is absolute pressure. The space velocity is space velocity by volume. [0028] According to the present invention, zinc oxide may be introduced to the support in various existing means. For example, it may be introduced by impregnation, or by kneading during forming, or by gelling and co-precipitation during 25 preparation of the support. Impregnation is preferred, i.e.: making a dissolvable compound of zinc into an impregnation liquid, then impregnating the support in the impregnation liquid and then drying and calcinating them. The dissolvable compound of zinc may be dissolvable inorganic salt and/or organic salt of zinc, such as: one or more of chloride, nitrate, sulfate, hydrochloride, acetate and citrate. As to element zinc, the concentration of the impregnation liquid is 5 g/L-300 g/L, preferably 20 g/L-200 g/L, more preferably 40 g/L-160 g/L. Impregnation in an equal volume or oversaturated 30 impregnation may be adopted. [0029] When the catalyst of the present invention further contains a promoter, the promoter may be introduced before, after or simultaneously with zinc oxide. It may be introduced by impregnation, or by kneading during forming, or by gelling and co-precipitation during preparation of the support. Impregnation is preferred, specifically: adopting a zinc salt and promoter metal salt solution to impregnate the formed support, drying and calcinating and then carrying out halogenation, 35 or adopting a zinc salt solution to impregnate the formed support at first, drying and calcinating and then carrying out halogenation, lastly impregnating in a promoter metal salt solution and then drying and calcinating to obtain halomethane, which is used to make isobutylene catalyst. [0030] The drying temperature may be 50°C-200°C, preferably 60°C-150°C, more preferably 80°C-120°C; the drying time is 1h-24h, preferably 4h-8h; the drying may be vacuum drying, or drying under protection of inert gas, or drying in 40 an air atmosphere; the calcination temperature is 200°C-800°C, preferably 400°C-600°C; the calcination time is 1h-24h, preferably 4h-8h; the calcination may be under protection of inert gas, or in an air atmosphere. [0031] The support may be an existing commercial product, or prepared by a method well known to those skilled in the art. The support may be prepared according to need or made into an appropriate granular shape, such as: bar, slice, cylinder or sphere. The forming may be based on general knowledge of the art. 45 [0032] The present invention also provides application of the supported catalyst of the present invention in the preparation of isobutylene. [0033] The present invention further provides a method for preparation of isobutylene from halomethane, including carrying out hydrogen reduction activation of the supported catalyst of the present invention to make the content of halogen in the activated catalyst be 20 wt.% -90 wt.% of the total content of halogen in the supported catalyst without 50 reduction, then contacting halomethane with the activated catalyst to prepare isobutylene. [0034] According to the present invention, the conditions of the hydrogen reduction activation make the content of halogen in the activated catalyst be preferably 30 wt.%-80 wt.% of the total content of halogen in the supported catalyst without reduction, more preferably 40 wt.%-80 wt.%. [0035] According to an embodiment of the present invention, the way of hydrogen reduction activation includes raising 55 temperature of the catalyst to 300°C-600°C in an inert atmosphere; then inputting hydrogen or a mixed gas of hydrogen and inert gas at a space velocity of 200h-1-2000h-1 and holding pressure at 0.1MPa-0.5MPa for 2h-16h. The volume percentage of hydrogen in the mixed gas is 10%-95%. Preferably, raising temperature to 350°C-550°C; then inputting hydrogen or a mixed gas of hydrogen and inert gas at a space velocity of 500h -1-1000h-1 and holding pressure at 0.1MPa-

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0.3MPa for 4h-8h. The volume percentage of hydrogen in the mixed gas is 30%-90%. [0036] According to the present invention, the halomethane may be one or more of monohalomethane, bihalomethane and trihalomethane, preferably, one or more of monobromomethane, bibromomethane and tribromomethane. [0037] Preferably, the contact conditions include reaction temperature 150°C-350°C, reaction pressure 0.1MPa-5MPa 5 and space velocity 50h -1-1000h-1; more preferably, reaction temperature 180°C-300°C, still more preferably 200-270°C; reaction pressure 0.1MPa-3MPa; space velocity 200h-1-500h-1. [0038] According to an embodiment of the present invention, the method for preparing isobutylene from halomethane includes raising temperature of the catalyst to 300°C-600°C in an inert atmosphere, preferably 350°C-550°C; then inputting hydrogen or a mixed gas of hydrogen and inert gas at a space velocity of 200h-1-2000h-1, preferably 500h-1- 10 1000h-1; and after treating at 0.1MPa-0.5MPa (absolute pressure), preferably 0.1MPa-0.3MPa (absolute pressure) for 2h-16h, preferably 4h-8h, lowering temperature to reaction temperature and inputting halomethane to take reaction. The volume percentage of hydrogen in the mixed gas is 10%-95%, preferably 30%-90%, more preferably 50%-90%. [0039] In the use of the present invention, the raw material may alternatively be a mixed gas of halomethane and inert gas, of which the volume concentration of halomethane is 10% -90%, preferably 30% -80%. 15 [0040] The inert gas involved in the use of the present invention is nitrogen, argon, helium and other gases that don’t take reaction under the conditions involved in the present invention, preferably nitrogen. [0041] According to the use of the present invention, the reaction for preparing isobutylene from halomethane may be conducted in any form of existing reactors, such as: reactors in form of fixed bed, fluidized bed, fixed fluidized bed, moving bed, slurry bed or bubbling bed, preferably fixed bed and fluidized bed reactors. 20 [0042] Thereafter, the present invention is further described by referring to examples, but they are not intended to limit the present invention. [0043] In the following examples and comparative examples, acid content is determined by NH3-TPD method. The adopted instrument is AutoChem 2920 chemical adsorption instrument of American MICROMERITICS. The concrete determination process is as follows: purging the sample with helium at 450°C for 1h, reducing temperature to 150°C, 25 introducing a mixed gas of ammonia and helium, with ammonia volume content of 10%, and carrying out pulse adsorption for five times to achieve a balance; purging with helium for 2h, and then raising temperature according to a temperature increase speed program of 10°C/min and conducting desorption of ammonia till 450°C; detecting ammonia by TCD detector after desorption and quantitatively calculating the acidity on catalyst surface. [0044] In the following examples and comparative examples, the content of element Br and that of element Zn are 30 determined by XRF (X-ray fluorescent spectroscopy) method. The adopted instrument is ZSX X-ray fluorescence spec-

trophotometer of Japanese Rigaku. The content of ZnBr 2 is calculated based on the content of element Br. The content of ZnO is calculated based on total Zn content minus the content of Zn in ZnBr 2.

Example 1 35 [0045] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 80°C for 8h and calcinate at 600°C for 4h to obtain catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with monobro- 40 momethane under the conditions of 250°C, 0.2 MPa (absolute pressure), 100h -1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-1. The weight composition of the catalyst is that the weight content of

ZnBr2 is 27%, the weight content of ZnO is 6%, the total acidity of 450°C or less in the catalyst is 0.92 mmol/g, and the acidity of 250°C-350°C is 55.1% of the total acidity of 450°C or less. [0046] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed 45 micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 50%. The reaction temperature is 230°C, reaction pressure is 1MPa (absolute pressure) and space velocity is 500h -1. Before input of feed gas, the catalyst is activated in a hydrogen atmosphere. The conditions of reduction are 400°C, 0.2MPa (absolute pressure) and 1000h -1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 67.51% of the total content of halogen in the catalyst before 50 reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 2

55 [0047] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 8h to obtain catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas

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of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h -1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-2. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO is 4%, the total acidity of 450°C or less in the catalyst is 0.93 mmol/g, and the acidity 5 of 250°C-350°C is 63.2% of the total acidity of 450°C or less. [0048] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed 10 atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 53.47% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

15 Example 3

[0049] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry under vacuum at 100°C for 8h and calcinate at 400°C for 8h to obtain catalyst 20 precursor ZnO/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 30% under the conditions of 300°C, 0.1MPa (absolute pressure), 500h-1 and 4h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-3. The weight composition of the obtained catalyst is that the weight

content of ZnBr2 as to bromide is 33%, the weight content of ZnO as to oxide is 2%, the total acidity of 450°C or less in 25 the catalyst is 0.95 mmol/g, and the acidity of 250°C-350°C is 75.5% of the total acidity of 450°C or less. [0050] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80%. The reaction temperature is 200°C, reaction pressure is 3MPa (absolute pressure) and space velocity is 350h-1. Before input of feed gas, the catalyst is activated in a mixed 30 atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 50%. The conditions of reduction are 500°C, 0.1MPa (absolute pressure) and 500h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 47.22% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

35 Example 4

[0051] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 8h to obtain catalyst precursor ZnO/Al 2O3. 40 Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with monobromomethane under the conditions of 200°C, 0.3MPa (absolute pressure), 300h -1 and 1h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-4. The weight composition of the obtained catalyst is that the weight

content of ZnBr2 as to bromide is 18%, the weight content of ZnO as to oxide is 2%, the total acidity of 450°C or less in the catalyst is 0.72 mmol/g, and the acidity of 250°C-350°C is 66.8% of the total acidity of 450°C or less. 45 [0052] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 30%. The reaction temperature is 270°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 350h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 70%. The conditions of reduction 50 are 350°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 6h. The content of halogen in the catalyst after reduction is 57.81% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 5 55 [0053] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 100°C for 6h and calcinate at 500°C for 6h under protection of nitrogen to obtain

6 EP 3 056 269 B1

catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70% under the conditions of 200°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-5. The weight composition of the obtained catalyst is that the weight 5 content of ZnBr2 as to bromide is 39%, the weight content of ZnO as to oxide is 6%, the total acidity of 450°C or less in the catalyst is 0.98mmol/g, and the acidity of 250°C-350°C is 64.1% of the total acidity of 450°C or less. [0054] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is monobromomethane. The reaction temperature is 270°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 350h -1. Before input of feed gas, the catalyst 10 is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 60%. The conditions of reduction are 550°C, 0.3MPa (absolute pressure) and 800h -1. The time of reduction is 8h. The content of halogen in the catalyst after reduction is 41.37% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

15 Example 6

[0055] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C in a nitrogen atmosphere for 4h and calcinate at 500°C in a nitrogen 20 atmosphere for 4h to obtain catalyst precursor ZnO/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with monobromomethane under the conditions of 250°C, 0.2MPa (absolute pressure), 100h-1 and 1h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-6. The weight composition of the obtained catalyst is that the weight content of ZnBr 2 as to bromide is 35%, the weight content of ZnO as to oxide is 9%, the total acidity of 450°C or less in the catalyst is 0.94 mmol/g, and the acidity of 250°C-350°C 25 is 57.3% of the total acidity of 450°C or less. [0056] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 50%. The reaction temperature is 230°C, reaction pressure is 0.1MPa (absolute pressure) and space velocity is 500h-1. Before input of feed gas, the catalyst is activated in a mixed 30 atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.2MPa (absolute pressure) and 1000h -1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 58.39% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

35 Example 7

[0057] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/Al 2O3. 40 Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 90% under the conditions of 300°C, 0.1MPa (absolute pressure), 500h -1 and 4h to obtain a catalyst for preparation of isobutylene from halomethane,

marked as C-7. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 20%, the weight content of ZnO as to oxide is 1%, the total acidity of 450°C or less in the catalyst is 0.79 mmol/g, and 45 the acidity of 250°C-350°C is 74.9% of the total acidity of 450°C or less. [0058] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80%. The reaction temperature is 200°C, reaction pressure is 3MPa (absolute pressure) and space velocity is 350h-1. Before input of feed gas, the catalyst is activated in a mixed 50 atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 90%. The conditions of reduction are 500°C, 0.1MPa (absolute pressure) and 500h-1. The time of reduction is 6h. The content of halogen in the catalyst after reduction is 51.94% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

55 Example 8

[0059] Weigh an appropriate amount of zinc nitrate and zirconium nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m 2/g, bar type, equivalent diameter 1.5 mm) support

7 EP 3 056 269 B1

by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO-Zr/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation 5 of isobutylene from halomethane, marked as C-8. The weight composition of the obtained catalyst is that the weight

content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of Zr as to element is 2%, the total acidity of 450°C or less in the catalyst is 0.97mmol/g, and the acidity of 250°C-350°C is 69.7% of the total acidity of 450°C or less. [0060] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed 10 micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst 15 after reduction is 39.14% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 9

20 [0061] Weigh an appropriate amount of zinc nitrate and cerium nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m 2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst

precursor ZnO-Ce/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane 25 is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-9. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of Ce as to element is 1%, the total acidity of 450°C or less in the catalyst is 0.91mmol/g, and the acidity of 250°C-350°C is 68.9% of the total acidity of 450°C or less. 30 [0062] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction 35 are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 63.73% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 10 40 [0063] Weigh an appropriate amount of zinc nitrate and lanthanum nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m 2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO-La/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst 45 precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-10. The weight composition of the obtained catalyst is that the weight

content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of La as to element is 0.5%, the total acidity of 450°C or less in the catalyst is 0.87 mmol/g, and the acidity of 250°C-350°C is 65.3% 50 of the total acidity of 450°C or less. [0064] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed 55 atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 62.72% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

8 EP 3 056 269 B1

Example 11

[0065] Weigh an appropriate amount of zinc nitrate and titanium nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m 2/g, bar type, equivalent diameter 1.5 mm) support 5 by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst

precursor ZnO-Ti/Al2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-11. The weight composition of the obtained catalyst is that the weight 10 content of ZnBr 2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of Ti as to element is 3%, the total acidity of 450°C or less in the catalyst is 0.96 mmol/g, and the acidity of 250°C-350°C is 63.4% of the total acidity of 450°C or less. [0066] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen 15 of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 53.62% of the total content of halogen in the catalyst before reduction. After the reaction has become 20 stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 12

[0067] Weigh an appropriate amount of zinc chloride, dissolve it in deionized water, support it to aluminum oxide (pore 25 volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h -1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, 30 marked as C-12. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the total acidity of 450°C or less in the catalyst is 0.87 mmol/g, and the acidity of 250°C-350°C is 65.7% of the total acidity of 450°C or less. [0068] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen 35 of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 47.89% of the total content of halogen in the catalyst before reduction. After the reaction has become 40 stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 13

[0069] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to silicon dioxide (pore 45 volume 1.06 ml/g, specific surface area 387 m 2/g, spherical shape, equivalent diameter 0.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/SiO 2. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h -1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, 50 marked as C-13. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the total acidity of 450°C or less in the catalyst is 1.08 mmol/g, and the acidity of 250°C-350°C is 49.7% of the total acidity of 450°C or less. [0070] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen 55 of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 400°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst

9 EP 3 056 269 B1

after reduction is 31.28% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 14 5 [0071] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to hydrogen-type ZSM- 5 (silica-alumina mole ratio 50, pore volume 0.23 ml/g, specific surface area 426 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/H-ZSM-5. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat 10 the catalyst precursor with mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-14. The weight composition of the obtained catalyst is that

the weight content of ZnBr 2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the total acidity of 450°C or less in the catalyst is 0.74 mmol/g, and the acidity of 250°C-350°C is 48.7% of the total acidity of 450°C or less. 15 [0072] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction 20 are 400°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 79.73% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 15 25 [0073] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas 30 of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h. Weigh an appropriate amount of zirconium nitrate, dissolve it in deionized water, impregnate bromized sample by the method of incipient wetness impregnation, dry at 120°C in a nitrogen atmosphere for 4h and calcinate at 500°C in a nitrogen atmosphere for 4h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-15. The weight composition of the obtained catalyst is that the weight 35 content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of Zr as to element is 1%, the total acidity of 450°C or less in the catalyst is 0.72 mmol/g, and the acidity of 250°C-350°C is 71.4% of the total acidity of 450°C or less. [0074] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen 40 of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 42.57% of the total content of halogen in the catalyst before reduction. After the reaction has become 45 stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 16

[0075] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore 50 volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 4h to obtain catalyst precursor ZnO/Al 2O3. Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h-1 and 2h. Weigh an appropriate amount of cerium nitrate, dissolve it in 55 deionized water, impregnate bromized sample by the method of incipient wetness impregnation, dry at 80°C in a nitrogen atmosphere for 8h and calcainate at 500°C in a nitrogen atmosphere for 4h to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-16. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the weight content of Ce as to

10 EP 3 056 269 B1

element is 0.5%, the total acidity of 450°C or less in the catalyst is 0.81 mmol/g, and the acidity of 250°C-350°C is 69.3% of the total acidity of 450°C or less. [0076] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen 5 of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 500h-1. The time of reduction is 6h. The content of halogen in the catalyst after reduction is 65.49% of the total content of halogen in the catalyst before reduction. After the reaction has become 10 stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Example 17

[0077] A supported catalyst is prepared and the reaction for preparing isobutylene from bromomethane takes place 15 according to the methods described in Example 16 except that aluminum oxide with pore volume of 0.51 ml/g, specific surface area of 162.4 m2/g, bar type and equivalent diameter of 1 mm is used as a support to obtain a catalyst for preparation of isobutylene from halomethane, marked as C-17. The total acidity of 450°C or less in the obtained catalyst is 0.72 mmol/g, and the acidity of 250°C-350°C is 70.5% of the total acidity of 450°C or less. The content of halogen in the catalyst after reduction activation is 72.57% of the total content of halogen in the catalyst before reduction. The 20 catalyst properties and reaction result are shown in Table 1.

Example 18

[0078] A supported catalyst is prepared and the reaction for preparing isobutylene from bromomethane takes place 25 according to the methods described in Example 16 excepte that bromomethane is substituted with dichloromethane in equalmolar weight. The result indicatesthe conversionrate of dichloromethane is97.4%, and the selectivity of isobutylene is 67.9%.

Comparative Example 1 30 [0079] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 8h to obtain catalyst ZnO/Al 2O3, marked as D-1. The weight composition of the obtained catalyst is that the weight content of ZnO as to oxide is 20%, the total 35 acidity of 450°C or less in the catalyst is 0.49 mmol/g, and the acidity of 250°C-350°C is 44.5% of the total acidity of 450°C or less. [0080] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 30%. The reaction temperature is 270°C, reaction pressure is 40 2MPa (absolute pressure) and space velocity is 350h -1. Before input of feed gas, the catalyst is activated in a hydrogen atmosphere. The volume content of hydrogen in the mixed gas is 70%. The conditions of reduction are 350°C, 0.3MPa (absolute pressure) and 800h -1. The time of reduction is 6h. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

45 Comparative Example 2

[0081] Weigh an appropriate amount of zinc nitrate, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 120°C for 4h and calcinate at 500°C for 8h to obtain catalyst precursor ZnO/Al 2O3. 50 Put 5g of the catalyst precursor in a continuous flow fixed bed reactor and treat the catalyst precursor with a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 80% under the conditions of 250°C, 0.3MPa (absolute pressure), 300h -1 and 2h to obtain a catalyst for preparation of isobutylene from halomethane, marked as D-2. The weight composition of the obtained catalyst is that the weight content of ZnBr2 as to bromide is 30%, the weight content of ZnO as to oxide is 4%, the total acidity of 450°C or less in the catalyst is 0.93 mmol/g, and 55 the acidity of 250°C-350°C is 63.2% of the total acidity of 450°C or less. [0082] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is

11 EP 3 056 269 B1

2MPa (absolute pressure) and space velocity is 200h -1. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1.

Comparative Example 3 5 [0083] Weigh an appropriate amount of zinc bromide, dissolve it in deionized water, support it to aluminum oxide (pore volume 0.71 ml/g, specific surface area 236 m2/g, bar type, equivalent diameter 1.5 mm) support by the method of incipient wetness impregnation, dry at 80°C in a nitrogen atmosphere for 4h and calcinate at 500°C in a nitrogen atmosphere for 4h to obtain catalyst ZnBr2/Al2O3, marked as D-3. The weight composition of the obtained catalyst is 10 that the weight content of ZnBr2 as to bromide is 30%, the total acidity of 450°C or less in the catalyst is 1.01 mmol/g, and the acidity of 250°C-350°C is 74.3% of the total acidity of 450°C or less. [0084] The reaction for preparation of isobutylene from bromomethane takes place in a continuous fluidized fixed bed micro-reactor. The loading amount of catalyst is 5g. The feed gas is a mixed gas of monobromomethane and nitrogen of which volume concentration of monobromomethane is 70%. The reaction temperature is 230°C, reaction pressure is 15 2MPa (absolute pressure) and space velocity is 200h-1. Before input of feed gas, the catalyst is activated in a mixed atmosphere containing hydrogen. The volume content of hydrogen in the mixed gas is 80%. The conditions of reduction are 450°C, 0.3MPa (absolute pressure) and 800h-1. The time of reduction is 4h. The content of halogen in the catalyst after reduction is 91.27% of the total content of halogen in the catalyst before reduction. After the reaction has become stable for one hour, samples are taken and analyzed. The reaction result is shown in Table 1. 20 Table 1 Catalyst reactivity zinc zinc Total Acid Isobutylene promoter Bromomethane Catalyst oxide halide Support acidity ratio selectivity, wt.% conversion rate, % wt.% wt.% mmol/g % % 25 27 C-16 0Al2O3 0.92 55.1 94.5 73.4 (ZnBr2) 30 C-24 0Al2O3 0.93 63.2 99.4 82.5 (ZnBr2) 30 33 C-32 0Al2O3 0.95 75.5 92.1 81.6 (ZnBr2) 18 C-42 0Al2O3 0.72 66.8 96.2 86.3 (ZnBr2) 35 39 C-56 0Al2O3 0.98 64.1 97.8 91.2 (ZnBr2) 35 C-69 0Al2O3 0.94 57.3 91.5 78.7 (ZnBr2 40 20 C-71 0Al2O3 0.79 74.9 91.4 82.7 (ZnBr2) 30 C-84 2(Zr) Al2O3 0.97 69.7 99.3 84.2 (ZnBr2) 45 30 C-94 1(Ce) Al2O3 0.91 68.9 98.5 88.2 (ZnBr2) 30 C-10 4 0.5(La) Al2O3 0.87 65.3 97.8 86.6 (ZnBr2) 50 30 C-11 4 3(Ti) Al2O3 0.96 63.4 95.9 88.5 (ZnBr2) 30 C-12 4 0Al2O3 0.87 65.7 95.4 84.3 (ZnBr2) 55 30 C-13 4 0SiO2 1.08 49.7 57.8 71.1 (ZnBr2)

12 EP 3 056 269 B1

(continued)

zinc zinc Total Acid Isobutylene promoter Bromomethane Catalyst oxide halide Support acidity ratio selectivity, wt.% conversion rate, % 5 wt.% wt.% mmol/g % % 30 C-14 4 0ZSM-5 0.74 48.7 92.6 52.2 (ZnBr2) 30 C-15 4 1(Zr) Al2O3 0.72 71.4 94.2 91.3 10 (ZnBr2) 30 C-16 4 0.5(Ce) Al2O3 0.81 69.3 92.5 86.7 (ZnBr2) 30 C-17 4 0.5(Ce) Al2O3 0.72 70.5 93.6 76.4 15 (ZnBr2)

D-12000Al2O3 0.49 44.5 99.7 0 30 D-24 0Al2O3 0.93 63.2 0 0 (ZnBr2) 20 30 D-30 0Al2O3 1.01 74.3 8.31 0 (ZnBr2)

[0085] The results in Table 1 indicate the catalyst of the present invention has obviously higher bromomethane conversion rate and isobutene selectivity. 25

Claims

1. A supported catalyst comprising a support and a metallic active component supported on the support; the metallic 30 active component contains zinc oxide and zinc halide, and the content of zinc oxide is 0.5 wt.%-20 wt.%, the content of zinc halide is 10 wt.%-50 wt.%, and the content of the support is 40 wt.%-88 wt.% based on the total weight of the catalyst.

2. The supported catalyst according to claim 1, wherein the content of zinc oxide is 1 wt.%-15 wt.%, the content of 35 zinc halide is 15 wt.%-40 wt.%, and the content of the support is 50 wt.%-84 wt.%, preferably, the content of zinc oxide is 1 wt.%-9 wt.%, the content of zinc halide is 18 wt.%-39 wt.%, and the content of the support is 55 wt.%-80 wt.% based on the total weight of the catalyst.

3. The supported catalyst according to claim 1 or 2, wherein the zinc halide is selected from one or more of zinc fluoride, 40 zinc chloride, zinc bromide and zinc iodide, and the support is selected from one or more of aluminum oxide, silicon oxide and ZSM-5 molecular sieve; preferably, the zinc halide is zinc bromide, and the support is aluminum oxide.

4. The supported catalyst according to any one of claims 1-3, further comprising a promoter selected from one or more of Ti, Zr, Ce and La, and the content of the promoter calculated on element is 0.1 wt.%-10 wt.% based on the total 45 weight of the catalyst.

5. The supported catalyst according to claim 4, wherein the promoter is Zr, and the weight content of the promoter calculated on element is 0.5 wt.%-5 wt.% based on the total weight of the catalyst.

50 6. The supported catalyst according to any one of claims 1-5, wherein it is determined by NH 3-TPD method by using the equipment and conditions as defined in the description that the total acidity at 450°C or less in the catalyst is 0.5 mmol/g-1.3 mmol/g, and the acidity at 250°C-350°C is 20%-90% of the total acidity at 450°C or less;

preferably, the total acidity at 450°C or less in the catalyst is 0.6 mmol/g-1.2 mmol/g, and the acidity at 250°C- 55 350°C is 30%-80% of the total acidity at 450°C or less; more preferably, the total acidity at 450°C or less in the catalyst is 0.7 mmol-1.1 mmol/g, and the acidity at 250°C-350°C is 40%-80% of the total acidity at 450°C or less.

13 EP 3 056 269 B1

7. A method for preparing a supported catalyst including the following steps: introducing zinc oxide to a support and then halogenating the resulted support after introducing zinc oxide,

wherein the means of halogenation includes contacting gaseous-phase halogen-containing compound with the 5 support containing the introduced zinc oxide, and the contact conditions make the zinc oxide on the support partially converted into zinc halide, and wherein the dose of zinc oxide makes the content of the support be 40%-88% based on the total weight of the obtained supported catalyst, and the contact conditions make the content of zinc oxide on the support be 0.5%- 20%, and the content of zinc halide be 10%-50%. 10 8. The method according to claim 7, wherein gaseous-phase halogen-containing compound contacts the support containing the introduced zinc oxide in a form of a mixed gas of gaseous-phase halogen-containing compound and inert gas, and the concentration of gaseous-phase halogen-containing compound in the mixed gas is not less than 20 v/v%. 15 9. The method according to claim 8, wherein the gaseous-phase halogen-containing compound is one or more of monohalomethane, bihalomethane and trihalomethane.

10. The method according to claim 8 or 9, wherein the means of contact includes putting the support containing the 20 introduced zinc oxide in a continuous flow fixed bed reactor, raising temperature to 150°C-400°C in an inert atmosphere, and inputting gaseous-phase halogen-containing compound or a mixed gas containing gaseous-phase halogen-containing compound with the space velocity 50h-1-1000 h-1, the contact pressure 0.1MPa-0.5MPa and the time 0.5h-8h; preferably, the temperature is raised to 180°C-350°C in an inert atmosphere, the space velocity is 100h-1-500h-1, the contact pressure is 0.1MPa-0.3MPa and the time is 1h-4h. 25 11. Use of the supported catalyst according to any one of claims 1-6 in the preparation of isobutylene.

12. A method for preparation of isobutylene from halomethane including carrying out hydrogen reduction activation of the supported catalyst according to any one of claims 1-6 to make the content of halogen in the activated catalyst 30 be 20 wt.%-90 wt.% of the total content of halogen in the supported catalyst without reduction, then contacting halomethane with the activated catalyst to prepare isobutylene.

13. The method according to claim 12, wherein the contact conditions include reaction temperature 150°C-350°C, reaction pressure 0.1MPa-5MPa and space velocity 50h -1-1000h-1; preferably, reaction temperature 180°C-300°C, 35 reaction pressure 0.1MPa-3MPa and space velocity 200h-1-500h-1.

14. The method according to claim 12, wherein the conditions of hydrogen reduction activation make the content of halogen in the catalyst be 30 wt.%-80 wt.% of the total content of halogen in the catalyst before reduction.

40 15. The method according to any one of claims 12-14, wherein the means of hydrogen reduction activation includes raising temperature of the catalyst to 300°C-600°C in an inert atmosphere; then inputting hydrogen or a mixed gas of hydrogen and inert gas in which the volume percentage of hydrogen in the mixed gas is 10%-95% at a space velocity of 200h-1-2000h-1 and holding pressure at 0.1MPa-0.5MPa for 2h-16h; preferably, raising temperature to 350°C-550°C; then inputting hydrogen or a mixed gas of hydrogen and inert gas in which the volume percentage 45 of hydrogen in the mixed gas is 30%-90% at a space velocity of 500h-1-1000h-1 and holding pressure at 0.1MPa- 0.3MPa for 4h-8h.

16. The method according to any one of claims 12-15, wherein halomethane is one or more of monohalomethane, bihalomethane and trihalomethane, preferably, one or more of monobromomethane, bibromomethane and tribro- 50 momethane.

17. The method according to any one of claims 12-16, wherein the contact takes place in a fixed bed, fluidized bed, fixed fluidized bed, moving bed, slurry bed or bubbling bed reactor.

55 Patentansprüche

1. Getragener Katalysator, enthaltend einen Träger und eine metallische aktive Komponente, die auf dem Träger

14 EP 3 056 269 B1

getragen ist; wobei die metallische aktive Komponente Zinkoxid und Zinkhalogenid enthält und der Gehalt von Zinkoxid 0,5 bis 20 Gew.-%, der Gehalt von Zinkhalogenid 10 bis 50 Gew.-% und der Gehalt des Trägers 40 bis 88 Gew.-% ist, bezogen auf das Gesamtgewicht des Katalysators.

5 2. Getragener Katalysator gemäß Anspruch 1, worin der Gehalt von Zinkoxid 1 bis 15 Gew.-%, der Gehalt von Zink- halogenid 15 bis 40 Gew.-% und der Gehalt des Trägers 50 bis 84 Gew.-% ist, bevorzugt der Gehalt von Zinkoxid 1 bis 9 Gew.-%, der Gehalt von Zinkhalogenid 18 bis 39 Gew.-% und der Gehalt des Trägers 55 bis 80 Gew.-% ist, bezogen auf das Gesamtgewicht des Katalysators.

10 3. Getragener Katalysator gemäß Anspruch 1 oder 2, worin das Zinkhalogenid ausgewählt ist aus einem oder mehreren von Zinkfluorid, Zinkchlorid, Zinkbromid und Zinkiodid und der Träger ausgewählt ist aus einem oder mehreren von Aluminiumoxid, Siliciumoxid und ZSM-5-Molekularsieb, bevorzugt das Zinkhalogenid Zinkbromid und der Träger Aluminiumoxid sind.

15 4. Getragener Katalysator gemäß einem der Ansprüche 1 bis 3, weiterhin enthaltend einen Promotor, ausgewählt aus einem oder mehreren von Ti, Zr, Ce und La und der Gehalt des Promotors, berechnet auf das Element, 0,1 bis 10 Gew.-% ist, bezogen auf das Gesamtgewicht des Katalysators.

5. Getragener Katalysator gemäß Anspruch 4, worin der Promotor Zr ist und der Gewichtsgehalt des Promotors, 20 berechnet auf das Element, 0,5 bis 5 Gew.% ist, bezogen auf das Gesamtgewicht des Katalysators.

6. Getragener Katalysator gemäß einem der Ansprüche 1 bis 5, worin gemäß NH 3-TPD-Verfahren durch Verwendung der Anlage und Bedingungen, wie in der Beschreibung definiert ist, die gesamte Azidität bei 450°C oder weniger im Katalysator 0,5 bis 1,3 mmol/g ist und die Azidität bei 250 bis 350°C 20 bis 90 % der gesamten Azidität bei 450°C 25 oder weniger ist, bevorzugt die gesamte Azidität bei 450°C oder weniger im Katalysator 0,6 bis 1,2 mmol/g und die Azidität bei 250 bis 350°C 30 bis 80 % der Gesamtazidität bei 450°C oder weniger ist, mehr bevorzugt die Gesamtazidität bei 450°C oder weniger im Katalysator 0,7 bis 1,1 mmol/g ist und die Azidität bei 250 bis 350°C 40 bis 80 % der Gesamtazidität bei 450°C oder weniger ist. 30 7. Verfahren zur Herstellung eines getragenen Katalysators, enthaltend die folgenden Schritte: Einführen von Zinkoxid zu einem Träger und anschließendes Halogenieren des resultierenden Trägers nach Einführen von Zinkoxid, worin das Mittel der Halogenierung das Kontaktieren einer Halogen-haltigen Verbindung in gasförmiger Phase mit dem Träger, der das eingefügte Zinkoxid enthält, aufweist und die Kontaktbedingungen zu einer teilweisen Um- 35 wandlung des Zinkoxids auf dem Träger zu Zinkhalogenid führen, und worin die Dosis des Zinkoxids den Gehalt des Trägers 40 bis 88 % ausmacht, bezogen auf das Gesamtgewicht des erhaltenen getragenen Katalysators, und die Kontaktbedingungen den Gehalt von Zinkoxid auf dem Träger 0,5 bis 20 % ausmachen und der Gehalt von Zinkhalogenid 10 bis 50 % wird.

40 8. Verfahren gemäß Anspruch 7, worin die Halogen-haltige Verbindung in Gasphase den Träger, der das eingefügte Zinkoxid enthält, in einer Form aus einem gemischten Gas aus einer Halogen-haltigen Verbindung in Gasphase und einem Inertgas kontaktiert und die Konzentration der Halogen-haltigen Verbindung in der Gasphase in dem gemischten Gas nicht weniger als 20 V/V-% ist.

45 9. Verfahren gemäß Anspruch 8, worin die Halogen-haltige Verbindung in Gasphase eine oder mehrere von Mono- halomethan, Bihalomethan und Trihalomethan ist.

10. Verfahren gemäß Anspruch 8 oder 9, worin das Mittel des Kontaktes das Geben des Trägers, der das eingeführte Zinkoxid enthält, in einen kontinuierlichen fixierten Fließbettreaktor enthält, Erhöhen der Temperatur auf 150 bis 50 400°C in einer Inertatmosphäre und das Eingeben einer Halogen-haltigen Verbindung in Gasphase oder eines gemischten Gases, das die Halogen-haltige Verbindung mit Gasphase enthält, mit einer Raumgeschwindigkeit von 50 bis 1.000 h-1, einem Kontaktdruck von 0,1 bis 0,5 MPa und einer Zeit von 0,5 bis 8 h enthält, bevorzugt die Temperatur auf 180 bis 350°C in einer Inertatmosphäre angehoben wird, die Raumgeschwindigkeit 100 bis 500 h-1, der Kontaktdruck 0,1 bis 0,3 MPa und die Zeit 1 bis 4 Stunden sind. 55 11. Verwendung des getragenen Katalysators gemäß einem der Ansprüche 1 bis 6 bei der Herstellung von Isobutylen.

12. Verfahren zur Herstellung von Isobutylen aus Halomethan, enthaltend das Durchführen einer Wasserstoff-Reduk-

15 EP 3 056 269 B1

tionsaktivierung des getragenen Katalysators gemäß einem der Ansprüche 1 bis 6, um den Gehalt von Halogen in dem aktivierten Katalysator auf 20 bis 90 Gew.-% des Gesamtgehaltes von Halogen im getragenen Katalysator ohne Reduktion einzustellen, anschließendes Kontaktieren von Halomethan mit dem aktivierten Katalysator, zur Herstellung von Isobutylen. 5 13. Verfahren gemäß Anspruch 12, worin die Kontaktbedingungen eine Reaktionstemperatur von 150 bis 350°C, Re- aktionsdruck von 0,1 bis 5 MPa und eine Raumgeschwindigkeit von 50 bis 1.000 h-1, bevorzugt eine Reaktions- temperatur von 180 bis 300°C, Reaktionsdruck von 0,1 bis 3 MPa und Raumgeschwindigkeit von 200 bis 500 h-1 enthalten. 10 14. Verfahren gemäß Anspruch 12, worin die Bedingungen der Wasserstoff-Reduktionsaktivierung den Gehalt von Halogen im Katalysator auf 30 bis 80 Gew.-% des Gesamtgehaltes von Halogen im Katalysator vor der Reduktion einstellen.

15 15. Verfahren gemäß einem der Ansprüche 12 bis 14, worin das Mittel der Wasserstoff-Reduktionsaktivierung das Erhöhen der Temperatur des Katalysators auf 300 bis 600°C in einer Inertatmosphäre, anschließendes Eingeben von Wasserstoff oder einem gemischten Gas aus Wasserstoff und Inertgas, worin der Volumenprozentsatz von Wasserstoff im gemischten Gas 10 bis 95 % ist, bei einer Raumgeschwindigkeit von 200 bis 2.000 h -1 und Halten des Drucks bei 0,1 bis 0,5 MPa für 2 bis 16 h enthält, bevorzugt Anheben der Temperatur auf 350 bis 550°C, 20 anschließendes Eingeben von Wasserstoff oder einem gemischten Gas aus Wasserstoff und Inertgas, worin der Volumenprozentsatz von Wasserstoff im gemischten Gas 30 bis 90 % ist, bei einer Raumgeschwindigkeit von 500 bis 1.000 h-1 und einem Haltedruck von 0,1 bis 0,3 MPa für 4 bis 8 h.

16. Verfahren gemäß einem der Ansprüche 12 bis 15, worin Halomethan ein oder mehrere von Monohalomethan, 25 Bihalomethan und Trihalomethan ist, bevorzugt ein oder mehrere von Monobrommethan, Bibrommethan und Tri- brommethan.

17. Verfahren gemäß einem der Ansprüche 12 bis 16, worin der Kontakt in einem fixierten Bett, Fließbett, fixierten Fließbett, Bewegbett, Aufschlämmungsbett oder Blasenbettreaktor durchgeführt wird. 30

Revendications

1. Catalyseur supporté comprenant un support et un composant métallique actif supporté sur le support ; le composant 35 métallique actif contient de l’oxyde de zinc et un halogénure de zinc, et la teneur en oxyde de zinc est de 0,5 % en poids à 20 % en poids, la teneur en halogénure de zinc est de 10% en poids à 50% en poids, et la teneur en support est de 40 % en poids à 88 % en poids sur la base du poids total du catalyseur.

2. Catalyseur supporté selon la revendication 1, dans lequel la teneur en oxyde de zinc est de 1 % en poids à 15 % 40 en poids, la teneur en halogénure de zinc est de 15 % en poids à 40 % en poids et la teneur en support est de 50 % en poids à 84 % en poids, de préférence, la teneur en oxyde de zinc est de 1 % en poids à 9 % en poids, la teneur en halogénure de zinc est de 18 % en poids à 39 % en poids, et la teneur en support est de 55 % en poids à 80 % en poids sur la base du poids total du catalyseur.

45 3. Catalyseur supporté selon la revendication 1 ou 2, dans lequel l’halogénure de zinc est sélectionné parmi un ou plusieurs du fluorure de zinc, du chlorure de zinc, du bromure de zinc et de l’iodure de zinc, et le support est sélectionné parmi un ou plusieurs de l’oxyde d’aluminium, de l’oxyde de silicium et d’un tamis moléculaire ZSM-5 ; de préférence, l’halogénure de zinc est le bromure de zinc, et le support est l’oxyde d’aluminium.

50 4. Catalyseur supporté selon l’une quelconque des revendications 1 à 3, comprenant en outre un promoteur sélectionné parmi un ou plusieurs de Ti, Zr, Ce et La, et la teneur en promoteur calculée sur base élémentaire est de 0,1 % en poids à 10 % en poids sur la base du poids total du catalyseur.

5. Catalyseur supporté selon la revendication 4, dans lequel le promoteur est Zr et la teneur pondérale en promoteur 55 calculée sur base élémentaire est de 0,5 % en poids à 5 % en poids sur la base du poids total du catalyseur.

6. Catalyseur supporté selon l’une quelconque des revendications 1 à 5, dans lequel il est déterminé par le procédé NH3-TPD en utilisant l’équipement et les conditions tels que définis dans la description que l’acidité totale à 450 °C

16 EP 3 056 269 B1

ou moins dans le catalyseur est de 0,5 mmole/g à 1,3 mmole/g, et que l’acidité entre 250 °C et 350 °C est de 20 % à 90 % de l’acidité totale à 450 °C ou moins ; que de préférence, l’acidité totale à 450 °C ou moins dans le catalyseur est de 0,6 mmole/g à 1,2 mmole/g, et que l’acidité entre 250 °C et 350 °C est de 30 % à 80 % de l’acidité totale à 450 °C ou moins ; 5 mieux encore, que l’acidité totale à 450 °C ou moins dans le catalyseur est de 0,7 mmol à 1,1 mmole/g, et que l’acidité entre 250 °C et 350 °C est de 40 % à 80 % de l’acidité totale à 450 °C ou moins.

7. Procédé de préparation d’un catalyseur supporté comprenant les étapes suivantes consistant à : introduire de l’oxyde de zinc sur un support et à halogéner ensuite le support obtenu après introduction d’oxyde de zinc, 10 dans lequel les moyens d’halogénation comprennent la mise en contact d’un composé contenant un halogène en phase gazeuse avec le support contenant l’oxyde de zinc introduit, et les conditions de contact font que l’oxyde de zinc sur le support est converti en halogénure de zinc, et dans lequel la dose d’oxyde de zinc fait que la teneur en support est de 40 % à 88 % sur la base du poids total du catalyseur supporté obtenu, et les conditions de contact font que la teneur en oxyde de zinc sur le support est de 15 0,5 % à 20 %, et que la teneur en halogénure de zinc est de 10 % à 50 %.

8. Procédé selon la revendication 7, dans lequel le composé contenant un halogène en phase gazeuse vient en contact avec le support contenant l’oxyde de zinc introduit sous la forme d’un gaz mixte de composé contenant un halogène en phase gazeuse et de gaz inerte, et la concentration de composé contenant un halogène en phase gazeuse dans 20 le gaz mixte n’est pas inférieure à 20 % en v/v.

9. Procédé selon la revendication 8, dans lequel le composé contenant un halogène en phase gazeuse est un ou plusieurs corps parmi un monohalométhane, un bihalométhane et un trihalométhane.

25 10. Procédé selon la revendication 8 ou 9, dans lequel les moyens de contact comprennent le placement du support contenant l’oxyde de zinc introduit dans un réacteur à lit fixe et à écoulement continu, l’augmentation de la température jusqu’entre 150 °C et 400 °C dans une atmosphère inerte, et l’insertion d’un composé contenant un halogène en phase gazeuse ou d’un gaz mixte contenant un composé contenant un halogène en phase gazeuse avec la vitesse spatiale de 50 h -1 à 1000 h -1, la pression de contact de 0,1 MPa à 0,5 MPa et le temps de 0,5 h à 8 h ; de préférence, 30 la température est augmentée jusqu’entre 180 °C et 350 °C dans une atmosphère inerte, la vitesse spatiale est de 100 h-1 à 500 h-1, la pression de contact est de 0,1 MPa à 0,3 MPa et le temps est de 1 h à 4 h.

11. Utilisation du catalyseur supporté selon l’une quelconque des revendications 1 à 6 dans la préparation d’isobutylène.

35 12. Procédé de préparation d’isobutylène à partir d’un halométhane comprenant la réalisation d’une activation par réduction d’hydrogène du catalyseur supporté selon l’une quelconque des revendications 1 à 6 pour faire en sorte que la teneur en halogène dans le catalyseur activé soit de 20 % en poids à 90 % en poids de la teneur totale en halogène dans le catalyseur supporté sans réduction, puis la mise en contact d’un halométhane avec le catalyseur activé pour préparer de l’isobutylène. 40 13. Procédé selon la revendication 12, dans lequel les conditions de contact comprennent une température réactionnelle de 150 °C à 350 °C, une pression réactionnelle de 0,1 MPa à 5 MPa et une vitesse spatiale de 50 h-1 à 1000h-1; de préférence, une température réactionnelle de 180 °C à 300 °C, une pression réactionnelle de 0,1 MPa à 3 MPa et une vitesse spatiale de 200 h-1 à 500 h-1. 45 14. Procédé selon la revendication 12, dans lequel les conditions d’activation par réduction d’hydrogène font que la teneur en halogène dans le catalyseur est de 30 % en poids à 80 % en poids de la teneur totale en halogène dans le catalyseur avant la réduction.

50 15. Procédé selon l’une quelconque des revendications 12 à 14, dans lequel les moyens d’activation par réduction d’hydrogène comprennent l’augmentation de la température du catalyseur jusqu’entre 300 °C et 600 °C dans une atmosphère inerte, puis l’insertion d’hydrogène ou d’un gaz mixte d’hydrogène et d’un gaz inerte dans lequel le pourcentage en volume d’hydrogène dans le gaz mixte est de 10 % à 95 % à une vitesse spatiale de 200 h-1 à 2 000 h-1, et le maintien de la pression entre 0,1 MPa et 0,5 MPa pendant 2 h à 16 h ; de préférence, l’augmentation 55 de la température jusqu’entre 350 °C et 550 °C ; puis l’introduction d’hydrogène ou d’un gaz mixte d’hydrogène et de gaz inerte dans lequel le pourcentage en volume d’hydrogène dans le gaz mixte est de 30 % à 90 % à une vitesse spatiale de 500 h-1 à 1000 h-1, et le maintien de la pression entre 0,1 MPa et 0,3 MPa pendant 4 h à 8 h.

17 EP 3 056 269 B1

16. Procédé selon l’une quelconque des revendications 12 à 15, dans lequel l’halométhane est un ou plusieurs parmi un monohalométhane, un bihalométhane et un trihalométhane, de préférence un ou plusieurs parmi un monobro- mométhane, un bibromométhane et un tribromométhane.

5 17. Procédé selon l’une quelconque des revendications 12 à 16, dans lequel le contact a lieu dans un lit fixe, un lit fluidisé, un lit fluidisé fixe, un lit mobile, un lit en suspension ou dans un réacteur à lit à bulles.

18 EP 3 056 269 B1

REFERENCES CITED IN THE DESCRIPTION

This list of references cited by the applicant is for the reader’s convenience only. It does not form part of the European patent document. Even though great care has been taken in compiling the references, errors or omissions cannot be excluded and the EPO disclaims all liability in this regard.

Patent documents cited in the description

• CN 101041609 A [0004] • US 4154969 A [0007] • CN 101284232 A [0004] • EP 1421992 A [0008] • US 4091038 A [0006] • US 20090163749 A [0009]

Non-patent literature cited in the description

•JIELIHE; TING XU ; ZHIHUIWANG. Angew. Chem. • IVAN M. LORKOVIC ; AYSEN YILMAZ ; GURKAN Int. Ed., 2012, vol. 51, 2438-2442 [0004] A. YILMAZ et al. Catalysis Today, 2004, vol. 98, 317-322 [0004]