Method for reusing methanol to olefins catalyst after service

Abstract

The present invention discloses a method for reusing a catalyst after service in a methanol to olefins process. The method comprises: (a) activating the catalyst after service at high temperature to obtain catalyst i; (b) exchanging the catalyst i in step (a) with an ammonium salt solution, and calcining again at high temperature to obtain catalyst ii; (c) mixing the catalyst ii in step (b) with water, and shearing at high speed to prepare a suspension 1; adding a molecular sieve and a binder to the suspension 1, and shearing at high speed to prepare a suspension 2; (d) spray-drying the suspension 2 to prepare a microsphere catalyst, and calcining to obtain a finished methanol to olefins catalyst. The method provided by the present invention can realize the resource utilization of the MTO catalyst after service, and solve the problem of utilizing the MTO catalyst after service in an efficient and green way, and the catalyst can still maintain a high catalytic performance when reused in the methanol to olefins reaction.

Description

Technical Field

[0001] The invention relates to a method for reusing a methanol to olefin catalyst after service. Background Art

[0002] Ethylene and propylene are important basic organic raw materials in the chemical industry and play a vital role in the modern petroleum and chemical industry. Since the growth rate of China's low-carbon olefin production capacity is lower than the growth rate of demand, the supply capacity of low-carbon olefins and downstream products is seriously insufficient, the market gap is huge, and the dependence on imports is high. It is expected that China's demand for ethylene and propylene will continue to grow steadily for a long time in the future. China's oil resources are short and the situation that oil supply depends largely on imports will not change. Under the increasingly tense situation of world oil, the importance of the process route of natural gas / coal to methanol to olefins is becoming increasingly apparent, which provides a new development direction for the situation where chemical raw materials are difficult to meet the development needs of traditional olefin production processes, and provides strong support for ensuring China's energy security.

[0003] The development of catalytic materials is the core of methanol to olefins technology. In 1984, Union Carbide Corporation (UCC) invented the silicoaluminophosphate molecular sieve (SAPO molecular sieve) with a pore size of about 0.4nm. SAPO molecular sieve is a crystal network structure composed of AlO4, SiO4 and PO4 tetrahedrons. The pores in the crystal are 4+ Replace P 5+ or Al 3+ The acidity generated by the reaction or the acidity generated by metal substitution. Among the SAPO series of molecular sieves, SAPO-34 molecular sieve is widely used in the modern petroleum processing industry because of its good thermal stability and hydrothermal stability, moderate acidity, high specific surface area and highly ordered micropore channels. The most eye-catching is that this molecular sieve is used as an active component in the methanol to olefins (MTO) reaction, which can almost completely convert methanol, with the selectivity of ethylene and propylene exceeding 80%, and C5 + The content of the components is relatively small and almost no aromatics are produced.

[0004] With the development of methanol to olefins technology, researchers and MTO enterprises are pursuing high product yields while also pursuing green products. Especially as environmental regulations become increasingly stringent, the resource utilization of post-service catalysts and the preparation of highly active methanol to olefins catalysts will effectively solve the problem of post-service catalyst accumulation in MTO enterprises. For an MTO unit with an annual methanol output of 1.8 million tons, more than 500 tons of post-service catalysts are produced each year. If this part of the catalyst can be recycled, it will not only promote the green development of the industry, but also meet the needs of SMTO enterprise users.

[0005] The catalyst in the MTO slurry tank comes from the water slurry containing the catalyst in the MTO separation tower. Since the mixed gas of the MTO reaction contains acidic impurity gases such as CO2, these acidic gases will corrode the equipment and pipelines; CO2 will also easily freeze into dry ice at low temperatures, which will block pipelines and equipment; in addition, the boiling point of acidic gases such as CO2 is close to that of hydrocarbons such as ethylene and propylene. If they are not removed, they will enter the final product of the separation unit, so the acidic gases need to be removed. MTO units usually use NaOH solution to wash the reaction mixed gas to achieve the purpose of removing acidic gases. Although acidic gases can be removed by injecting alkali, alkali metals will be introduced into the subsequent system and adsorbed on the catalyst after service, affecting the resource efficiency of the catalyst after service.

[0006] Regarding the utilization of post-service MTO catalysts, CN201410575041.3, a method for removing methanol by adsorption using waste SAPO-34 molecular sieve catalysts, and CN201410573567.8, a method for preparing an adsorbent and removing methanol from waste catalysts containing molecular sieves, propose that waste catalysts containing SAPO-34 be prepared into adsorbents by rolling, tableting or extruding, and used to remove methanol and other oxygen-containing compounds from olefin raw materials. However, such methods still have the problem of low utilization of post-service MTO catalysts, and they cannot be recycled as catalysts. Summary of the invention

[0007] The technical problem to be solved by the present invention is the utilization problem of methanol to olefins catalyst after service in the prior art. A new method for recycling methanol to olefins catalyst after service is provided. The method can realize the resource utilization of MTO catalyst after service, and solve the utilization problem of MTO catalyst after service in an efficient and green way. Moreover, the catalyst can still maintain high catalytic performance when reused in methanol to olefins reaction.

[0008] The present invention provides a method for reusing a methanol to olefins catalyst after service, comprising:

[0009] (a) activating the catalyst after service at high temperature to obtain catalyst i;

[0010] (b) exchanging the catalyst i from step (a) with an ammonium salt solution and calcining again at high temperature to obtain catalyst ii;

[0011] (c) mixing the catalyst ii from step (b) with water and subjecting them to high-speed shearing to prepare a suspension 1; adding a molecular sieve and a binder to the suspension 1 and subjecting them to high-speed shearing to prepare a suspension 2;

[0012] (d) spray drying the suspension 2 to prepare a microsphere catalyst, and calcining to obtain a finished methanol to olefin catalyst.

[0013] In the above technical solution, in step (a), the catalyst after service is a waste catalyst collected from a slurry tank of a methanol to olefins industrial device.

[0014] In the above technical solution, the catalyst after service in step (a) contains SAPO-34 molecular sieve, and the silicon-aluminum molar ratio of the SAPO-34 molecular sieve is SiO2:Al2O3=1:(2-10).

[0015] In the above technical solution, before use, the catalyst after service described in step (a) has a SAPO-34 molecular sieve content of 10 to 60 wt.% and a kaolin content of 10 to 70 wt.%.

[0016] In the above technical solution, the content of alkali metal elements in the catalyst after service in step (a) is not less than 1 wt.%, preferably 2-5 wt.%.

[0017] In the above technical solution, the particle size of the catalyst after service in step (a) is 15 to 100 microns; the specific surface area is not less than 150m 2 / g, pore volume not less than 0.1cm 3 / g, preferably with a specific surface area of ​​150 to 350 m 2 / g, pore volume is 0.1~0.25cm 3 / g.

[0018] In the above technical solution, in step (a), the high temperature activation condition is: activation at 500-700° C. for 2-6 hours in an air atmosphere.

[0019] In the above technical scheme, in step (b), the number of ammonium exchanges during the ammonium exchange process is not less than twice, preferably 2 to 5 times, the ammonium salt concentration is 2 to 30 wt.%, the solid-liquid mass ratio is 1: (5 to 30), the treatment temperature is 30 to 90°C, and the treatment time is 3 to 20 hours. The ammonium salt is selected from at least one of ammonium nitrate, ammonium chloride, and ammonium sulfate. After the ammonium exchange is completed, the sample is filtered, washed with deionized water, and dried, and the drying conditions are: temperature 90 to 150°C, time 5 to 24 hours.

[0020] In the above technical solution, in step (b), the high temperature calcination conditions are: activation at 500-700° C. for 2-6 hours in an air atmosphere.

[0021] In the above technical solution, in step (c), the molecular sieve is SAPO-18, SAPO-34, or SAPO-18 / SAPO-34 composite molecular sieve.

[0022] In the above technical solution, in step (c), the catalyst ii of step (b) and water are mixed and the suspension 1 is treated with high-speed shearing to achieve uniform mixing, until at least 90% of the particles in the suspension 1 have a size of 10 to 15 microns, and the high-speed shearing time is 0.1 to 2 hours.

[0023] In the above technical scheme, at least 90% of the particles in the suspension 2 after high-speed shearing in step (c) have a size of no more than 8 microns; preferably, in step (c), the binder is first added to the suspension 1, high-speed shearing is maintained, and then the molecular sieve is added and high-speed shearing is continued, and the high-speed shearing time before and after is 0.2 to 1h and 0.2 to 0.8h respectively, wherein at least 90% of the particles in the suspension 2 obtained after high-speed shearing have a size of no more than 8 microns.

[0024] In the above technical solution, in step (c), the binder is selected from inorganic sols, including silica sol, alumina sol, water glass, etc.

[0025] In the above technical solution, in step (c), the solid content of the suspension 2 is 20wt.% to 50wt.%.

[0026] In the above technical solution, in step (d), the spray drying conditions are: the drying temperature is 150-200°C.

[0027] In the above technical solution, in step (d), the calcination temperature is 500-600° C., and the calcination time is 3-8 hours.

[0028] The second aspect of the present invention also provides a methanol to olefins catalyst prepared by the above preparation method.

[0029] In the above technical solution, the wear index of the methanol to olefins catalyst is 1wt.% to 10wt.%.

[0030] In the above technical solution, the content of alkali metal elements in the methanol to olefins catalyst is 0.01wt.% to 0.5wt.%.

[0031] The third aspect of the present invention further provides a use of the methanol to olefins catalyst provided by the second aspect in a methanol to olefins reaction.

[0032] In the above technical solution, the olefin includes ethylene and / or propylene.

[0033] In the above technical scheme, methanol is used as raw material, the reaction temperature is 400-700°C, the reaction pressure is 0.1MPa-3MPa, and the reaction weight space velocity is 1-10h -1 Under the condition that the water / raw material weight ratio is 0 to 0.6, the raw material contacts the catalyst through the catalyst bed to react and generate olefins.

[0034] Compared with the prior art, the present invention has the following advantages:

[0035] 1. In the method provided by the present invention, the inventor innovatively discovered that the catalyst in the collected slurry tank is firstly removed from organic matter by roasting, and then the alkali metal ions such as Na are removed by ammonium exchange, and then the served catalyst after high-temperature activation is added in the subsequent preparation process of the MTO catalyst. By controlling the addition method and amount of the served catalyst, the utilization problem of the served MTO catalyst can be effectively solved under the premise of meeting the high activity and wear resistance of the catalyst, especially the resource utilization problem of the served MTO catalyst in the slurry tank can be solved.

[0036] 2. The method for resource utilization of spent catalysts in a methanol to olefins industrial device provided by the present invention has a simple operation process, and only requires replacing the carrier with spent MTO catalyst in the preparation process of a conventional methanol to olefins catalyst.

[0037] 3. The methanol to olefins catalyst prepared by the present invention exhibits good activity and high diene selectivity in the methanol to olefins reaction. DETAILED DESCRIPTION

[0038] As an implementation mode of the present invention, it should be pointed out that the protection scope of the present invention is not limited by these specific implementation modes, but is determined by the claims in the appendix.

[0039] In the present invention, the method for determining the wear index is as follows: under the jetting action of high-speed air flow, the microsphere catalyst is in a fluidized state, and wear occurs between the catalyst particles and between the catalyst and the vessel wall due to friction and collision. Fine powder will be carried away from the fluidizing chamber by the air flow and collected in the powder collection system. The wear index of the catalyst is obtained by calculating the amount of solid lost per unit time.

[0040] In the present invention, the specific surface area and pore volume are measured on a physical adsorption instrument. The solid particles present in a gas atmosphere will physically adsorb gas molecules on their external and internal micropore surfaces at low temperatures. By measuring the change in the equilibrium adsorption amount of nitrogen by the solid with the partial pressure of the gas at liquid nitrogen temperature, the adsorption isotherm of the solid adsorbent can be obtained, and the specific surface area of ​​the solid sample can be further obtained according to the BET equation. According to the adsorption amount of nitrogen by the solid at P / P0 close to 1, the total pore volume of the sample is obtained.

[0041] In the present invention, the particle size distribution is measured on a laser particle size analyzer. The operation method is as follows: the sample is evenly dispersed in water, the sample is evenly dispersed by mechanical stirring, and the sample circulating fluid is circulated through the sample pool. A beam of laser light of a specific wavelength emitted by the laser becomes a single parallel beam after passing through a lens. The beam irradiates the particle sample in the sample pool to cause diffraction, and the particle size and particle size distribution law of the particle are obtained according to the change in the intensity of the diffracted light of the particle at each angle.

[0042] The present invention will be further described below by means of specific examples.

[0043] [Example 1]

[0044] Catalyst after service:

[0045] The catalyst after service is selected from the waste catalyst collected from the slurry tank of the methanol to olefins industrial device, and the composition of the catalyst is 45% (weight) SAPO-34 molecular sieve: 45% (weight) kaolin: 10% (weight) binder. The silicon-aluminum ratio of SAPO-34 molecular sieve SiO2: Al2O3 is 1:5, the total alkali metal content is 3.5wt.%, and the specific surface area is 190m 2 / g, pore volume is 0.13cm 3 / g.

[0046] Preparation of methanol to olefins catalyst.

[0047] The raw materials are weighed according to the ratio of 20% (by weight) SAPO-34 molecular sieve: 20% (by weight) treated post-service catalyst: 5% (by weight) aluminum sol: 55% (by weight) deionized water. Except for water, the raw material ratios are all dry weight ratios.

[0048] The treatment of the catalyst after service is first high-temperature activation and then two ammonium exchanges. The high-temperature activation conditions are: temperature 650°C, time 4h, air flow rate 1L / min; the ammonium exchange conditions are: ammonium chloride, concentration 5wt.%, solid-liquid mass ratio 1:10, exchange time 5h, temperature 60°C. After the exchange, the sample is dried and calcined to obtain the treated service catalyst. The drying conditions are: temperature 100°C, time 10h; the calcination conditions are: temperature 650°C, time 4h, air flow rate 1L / min. The treated service catalyst was added to water and mixed evenly, and sheared for 30 minutes with a shearing machine to obtain suspension 1, in which 90% of the particles in suspension 1 had a size of 10 to 15 microns, aluminum sol was added, and shearing was continued for 30 minutes, and SAPO-34 molecular sieve was added, and shearing was continued for 15 minutes until a uniform suspension 2 was obtained, in which 90% of the particles in suspension 2 had a size of no more than 8 microns, and the solid content of suspension 2 was 38wt.%, and then the suspension was spray-dried at a temperature of 180°C, and then the catalyst obtained by spray drying was sent to a muffle furnace, and calcined at 550°C for 6 hours to obtain a methanol to olefins catalyst, and the obtained product was recorded as A. The wear index of the catalyst A was 3.5wt.%, and the alkali metal content was 0.05wt.%.

[0049] [Example 2]

[0050] Preparation of methanol to olefins catalyst.

[0051] The same as [Example 1], except that the raw materials are weighed according to the ratio of 17% (weight) SAPO-34 molecular sieve: 25% (weight) treated post-service catalyst: 5% (weight) aluminum sol: 53% (weight) deionized water. The treatment of the post-service catalyst is first high-temperature activation, and then three ammonium exchanges, the high-temperature activation conditions are: temperature 650°C, time 4h, air flow rate 1L / min; ammonium exchange conditions are: ammonium chloride, concentration is 5wt.%, solid-liquid mass ratio is 1:10, exchange time is 5h, temperature is 60°C, the exchanged sample is dried and roasted to obtain the treated service catalyst, wherein the drying conditions are: temperature 110°C, time 15h; roasting conditions are temperature: 650°C, time 5h, air flow: 1L / min. The treated service catalyst was added with water and mixed evenly, and sheared with a shearing machine for 30 minutes to obtain suspension 1, in which 90% of the particles in suspension 1 were 10-15 microns in size, aluminum sol was added, and shearing was continued for 30 minutes, and SAPO-34 molecular sieve was added, and shearing was continued for 15 minutes until a uniform suspension 2 was obtained, in which 90% of the particles in suspension 2 were not larger than 8 microns in size, and the solid content of suspension 2 was 42wt.%, and then the suspension was spray-dried at a temperature of 190°C, and then the catalyst obtained by spray drying was sent to a muffle furnace, and after calcination at 550°C for 6 hours, a methanol to olefins catalyst was obtained, and the obtained product was recorded as B. The wear index of the catalyst B was 2.8wt.%, and the alkali metal content was 0.1wt.%.

[0052] [Example 3]

[0053] Preparation of methanol to olefins catalyst.

[0054] The same as [Example 1], except that the aluminum sol is replaced by silica sol, and the raw materials are weighed according to the ratio of 20% (weight) SAPO-34 molecular sieve: 20% (weight) treated post-service catalyst: 5% (weight) silica sol: 55% (weight) deionized water. The treatment of the service catalyst is first high-temperature activation, and then two ammonium exchanges, the high-temperature activation conditions are: temperature 650°C, time 4h, air flow rate 1L / min; ammonium exchange conditions are: ammonium chloride, concentration is 5wt.%, solid-liquid mass ratio is 1:10, exchange time is 5h, temperature is 60°C, the exchanged sample is dried and roasted to obtain the treated service catalyst, wherein the drying conditions are: temperature 110°C, time 15h; roasting conditions are temperature: 650°C, time 5h, air flow: 1L / min. The treated service catalyst was added with water and mixed evenly, and sheared with a shearing machine for 30 minutes to obtain suspension 1, in which 90% of the particles in suspension 1 were 10-15 microns in size, aluminum sol was added, and shearing was continued for 30 minutes, and SAPO-34 molecular sieve was added, and shearing was continued for 15 minutes until a uniform suspension 2 was obtained, in which 90% of the particles in suspension 2 were not larger than 8 microns in size, and the solid content of the suspension was 38wt.%, and then the suspension 2 was spray-dried at a temperature of 160°C, and then the catalyst obtained by spray drying was sent to a muffle furnace, and after calcination at 550°C for 6 hours, a methanol to olefins catalyst was obtained, and the obtained product was recorded as C. The wear index of the catalyst C was 3wt.%, and the alkali metal content was 0.2wt.%.

[0055] [Comparative Example 1]

[0056] Preparation of methanol to olefins catalyst.

[0057] The raw materials are weighed according to the ratio of 20% (weight) SAPO-34 molecular sieve: 20% (weight) kaolin: 5% (weight) aluminum sol: 55% (weight) deionized water. Except for water, the raw material ratios are all dry weight ratios. SAPO-34 molecular sieve, kaolin, and binder are added to water and mixed evenly, and sheared with a shearing machine for 60 minutes to obtain a uniform suspension, in which 90% of the particle size in the suspension is not greater than 8 microns, and the solid content of the suspension is 36wt.%. The suspension is then spray-dried at a temperature of 180°C, and the catalyst obtained by spray drying is then sent to a muffle furnace, and a methanol to olefin catalyst is obtained after calcination at 550°C for 6 hours. The obtained product is recorded as D. The wear index of the catalyst D is 3.5wt.%. The alkali metal content is 0.6wt.%.

[0058] [Comparative Example 2]

[0059] Preparation of methanol to olefins catalyst.

[0060] The raw materials are weighed according to the ratio of 20% (by weight) SAPO-34 molecular sieve: 20% (by weight) treated post-service catalyst: 5% (by weight) aluminum sol: 55% (by weight) deionized water. Except for water, the raw material ratios are all dry weight ratios.

[0061] The treatment of the serving catalyst is first high-temperature activation, and then two ammonium exchanges. The high-temperature activation conditions are: temperature 650℃, time 4h, air flow rate 1L / min; ammonium exchange conditions are: ammonium chloride, concentration 5wt.%, solid-liquid mass ratio 1:10, exchange time 5h, temperature 60℃. After the exchange, the sample is dried and calcined to obtain the treated high-temperature serving catalyst, wherein the drying conditions are: temperature 110℃, time 15h; calcination conditions are temperature: 650℃, air flow rate: 1L / min. The treated serving catalyst, SAPO-34 molecular sieve and binder are added to water and mixed evenly, and sheared with a shearing machine for 90 minutes until a uniform suspension is obtained, 90% of the particle size in the suspension is not greater than 8 microns, and the solid content of the suspension is 38wt.%, and then the suspension is spray-dried at a temperature of 180℃, and then the catalyst obtained by spray drying is sent to a muffle furnace, and after calcining at 550℃ for 6 hours, a methanol to olefins catalyst is obtained, and the obtained product is recorded as E. The attrition index of the catalyst E was 6.3 wt.%. The alkali metal content was 0.1 wt.%.

[0062] [Comparative Example 3]

[0063] Preparation of methanol to olefins catalyst.

[0064] The raw materials are weighed according to the ratio of 20% (by weight) SAPO-34 molecular sieve: 20% (by weight) post-service catalyst after high temperature activation: 5% (by weight) aluminum sol: 55% (by weight) deionized water. Except for water, the raw material ratios are all dry weight ratios.

[0065] The catalyst after service is a high-temperature activated service catalyst obtained by high-temperature activation of the catalyst in the slurry tank, wherein the high-temperature activation conditions are temperature: 650°C, time 4h, air flow rate: 1L / min. The activated service catalyst is added to water and mixed evenly, and sheared with a shearing machine for 30 minutes to obtain a suspension 1, in which 90% of the particles in the suspension 1 have a size of 10 to 15 microns, aluminum sol is added, and shearing is continued for 30 minutes, and then molecular sieves are added and shearing is continued for 15 minutes until a uniform suspension 2 is obtained, in which 90% of the particles in the suspension 2 have a size of no more than 8 microns, and the solid content of the suspension 2 is 38wt.%, and then the suspension is spray-dried at a temperature of 180°C, and then the catalyst obtained by spray drying is sent to a muffle furnace, and a methanol to olefins catalyst is obtained after calcination at 550°C for 6 hours, and the obtained product is recorded as F. The wear index of the catalyst F is 2.8wt.%, and the alkali metal content is 1.3wt.%.

[0066] [Example 4]

[0067] The catalysts obtained in [Example 1-3] and [Comparative Example 1-3] were used in the methanol to olefin reaction. A fixed fluidized bed catalytic reaction device was used, and the reactor was a stainless steel tube. The process conditions used in the investigation were: catalyst loading 40.0 g, reaction temperature 480 ° C, weight space velocity 6 h -1 , pressure 0.1MPa, the evaluation results are shown in Table 1. In the present invention, the yield of each product is based on mass. The life of the catalyst in Table 1 is the time when the diene selectivity is at the highest point in the gas phase product analysis results, and the gas phase product analysis results are the results when the diene selectivity is at the highest point.

[0068] Table 1 Catalytic performance

[0069]

Claims

1. A method for reusing a methanol to olefins catalyst after service, comprising: (a) activating the catalyst after service at high temperature to obtain catalyst i; (b) exchanging the catalyst i from step (a) with an ammonium salt solution and calcining again at high temperature to obtain catalyst ii; (c) mixing the catalyst ii from step (b) with water and subjecting them to high-speed shearing to prepare a suspension 1; adding a molecular sieve and a binder to the suspension 1 and subjecting them to high-speed shearing to prepare a suspension 2; (d) spray drying the suspension 2 to prepare a microsphere catalyst, and calcining to obtain a finished methanol to olefin catalyst.

2. The method according to claim 1, characterized in that In step (a), the catalyst after service is a waste catalyst collected from a slurry tank of a methanol to olefins industrial device.

3. The method according to claim 1, characterized in that The catalyst after service in step (a) contains SAPO-34 molecular sieve, and the silicon-aluminum molar ratio of the SAPO-34 molecular sieve is SiO2:Al2O3=1:(2-10).

4. The method according to claim 1, characterized in that: Before use, the catalyst after service in step (a) has a SAPO-34 molecular sieve content of 10 to 60 wt.% and a kaolin content of 10 to 70 wt.%.

5. The method according to claim 1, characterized in that: In the catalyst after service in step (a), the content of alkali metal elements is not less than 1 wt.%.

6. The method according to claim 1, characterized in that In the catalyst after service in step (a), the content of alkali metal elements is 2-5 wt.%.

7. The method according to claim 1, characterized in that In step (a), the high temperature activation condition is: activation at 500-700° C. for 2-6 hours in an air atmosphere.

8. The method according to claim 1, characterized in that In step (c), the molecular sieve is SAPO-18, SAPO-34, or SAPO-18 / SAPO-34 composite molecular sieve.

9. The method according to claim 1, characterized in that: In step (c), the catalyst ii of step (b) and water are mixed and the suspension 1 is treated by high-speed shearing to achieve uniform mixing, until at least 90% of the particles in the suspension 1 have a size of 10 to 15 microns, and the high-speed shearing time is 0.1 to 2 hours; at least 90% of the particles in the suspension 2 after high-speed shearing have a size of no more than 8 microns.

10. The method according to claim 1, characterized in that In step (c), the solid content of the suspension 2 is 20 wt.% to 50 wt.%.

11. The method according to claim 1, characterized in that: In step (d), the spray drying conditions are: the drying temperature is 150-200° C.; the roasting temperature is 500-600° C., and the roasting time is 3-8 hours.

12. A methanol to olefins catalyst prepared by the method according to any one of claims 1 to 11.

13. The catalyst according to claim 12, characterized in that The wear index of the methanol to olefins catalyst is 1 wt.% to 10 wt.%.

14. The catalyst according to claim 12, characterized in that The content of alkali metal elements in the methanol to olefins catalyst is 0.01 wt.% to 0.5 wt.%.

15. Use of the methanol to olefins catalyst according to any one of claims 12 to 14 in a methanol to olefins reaction.

16. The use according to claim 15, characterized in that The olefins include ethylene and / or propylene; methanol is used as the raw material, the reaction temperature is 400-700°C, the reaction pressure is 0.1MPa-3MPa, the reaction weight space velocity is 1-10h -1 Under the condition that the water / raw material weight ratio is 0 to 0.6, the raw material contacts the catalyst through the catalyst bed to react and generate olefins.

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