CN101792362A - Method and device for continuously aromatizing dimethyl ether and regenerating catalyst - Google Patents

Abstract

The invention discloses a method and device for continuous aromatization of dimethyl ether and regeneration of a catalyst, belonging to the field of chemical industry, and in particular to a method for preparing aromatic hydrocarbons by aromatization of dimethyl ether, a catalyst and a method for regeneration thereof, and related reaction devices. Using a specific catalyst, the continuous aromatization reaction and catalyst regeneration are carried out in a certain combination of reactors (fixed bed, moving bed and fluidized bed). The device, catalyst and method can be used to process pure dimethyl ether or mixed raw materials containing dimethyl ether, and can adjust the activity of the catalyst in the aromatization reactor to achieve continuous and efficient conversion of dimethyl ether and high selectivity to generate aromatics. Purpose.

Description

Method and device for continuous aromatization of dimethyl ether and catalyst regeneration

technical field

The invention relates to a method for preparing aromatic hydrocarbons through aromatization of dimethyl ether, a catalyst and a device, and belongs to the field of chemical industry.

Background technique

Aromatics are one of the most important basic chemicals. In the traditional chemical route, aromatics are mainly obtained from petroleum refining and coal dry distillation. The aromatic hydrocarbons obtained by the petroleum route have high purity and are suitable for the preparation of various high-quality chemicals. The aromatics obtained by the coal (carbonization) route contain thiophene impurities, the quality is relatively low, and the application is limited. With the increasing shortage of petroleum resources, the supply of aromatics is tense, and the price remains high, which greatly increases the production of subsequent chemicals. costs, affecting sales. The use of natural gas (mainly composed of methane) or petroleum refinery dry gas (mainly containing methane, ethane, ethylene) and petroleum liquefied gas or methanol to produce aromatics is a relatively new technical route.

In particular, raw materials such as methanol can be prepared from coal or natural gas gasification and methanol synthesis, which has the advantages of large quantity and low cost. And its activity is relatively high, and it can pass through metal and molecular sieve composite catalyst at 350-500 °C Complete conversion is more convenient and efficient than methane, propane, ethane, etc. to produce aromatics. However, in the process of methanol aromatization reaction to generate aromatics, a large amount of aromatic hydrocarbons are generated at the same time. In this way, in a high temperature environment, water vapor will adversely affect the activity of the catalyst containing molecular sieves (including affecting the adsorption of other hydrocarbons and causing the molecular sieves to dealuminate and lose their activity). During the long-term reaction process, the acidity of the catalyst will be greatly reduced, and the activity cannot be effectively recovered, and the life of the catalyst will be greatly shortened. Although there are some methods reported in the literature that can supplement aluminum to molecular sieves, these methods all require no metal on the catalyst, which is obviously not suitable for the requirements of the aromatization system.

At present, although there are patent reports that methanol dehydration can generate dimethyl ether, there is no reactor technology and method for direct aromatization of dimethyl ether as a practical raw material.

Contents of the invention

In order to overcome the deficiencies of the above-mentioned methanol aromatization process, the object of the invention is to provide a method and device for directly carrying out continuous aromatization with dimethyl ether. The aromatization of dimethyl ether is compared with the aromatization of methanol, The amount of water generated in the process is greatly reduced, so the above problems are effectively alleviated. It is characterized by:

A method for catalytic conversion of dimethyl ether to synthesize aromatic hydrocarbons. It is characterized in that gas containing dimethyl ether is passed into a reactor equipped with a metal-molecular sieve composite catalyst, and aromatic hydrocarbons are generated at a certain temperature and pressure. After the catalyst is deactivated, the atmosphere is replaced for in-situ regeneration or the catalyst is moved to the catalyst regeneration reactor for regeneration, and then returned to the aromatization reactor, and the above process is repeated to obtain aromatics continuously.

The gas raw material of dimethyl ether as claimed in claim 1 among the present invention is characterized in that, this raw material can be pure dimethyl ether, also can be dimethyl ether and other components (methanol, water, C ₁ -C ₅ hydrocarbons, CO, CO ₂ , H ₂ ), these components can exist independently or simultaneously, and the total mass fraction of these components is not more than 50%.

In the present invention, as claimed in claim 1, the catalyst suitable for converting the gaseous raw material as claimed in claim 2 is characterized in that its structure is a complex of metal, molecular sieve, structural stabilizer or reinforcing agent. The types of metals include zinc, silver, molybdenum, copper, nickel, manganese, chromium, platinum, iron, ruthenium, tungsten, vanadium, osmium, etc. The metal loaded on the molecular sieve can be a single component, or a composite of two or more metals. The total load of metal is 0.5%-10% of the total mass of the catalyst. The skeleton components of the molecular sieve are silicon, aluminum, phosphorus, etc., and the proportion of pores with a pore diameter of 0.5-0.7nm in the molecular sieve is greater than 50%. The molecular sieve accounts for 50%-70% of the overall weight of the catalyst, and the others are structural stabilizers and reinforcing agents, and the Mohs hardness of the catalyst used is greater than 5. The average diameter of the catalyst particles is 0.05-0.5mm and 3-8mm.

The reactor according to claim 1 of the present invention comprises an aromatization reactor and a catalyst regeneration reactor. It is characterized in that when using a catalyst with a particle size of 3-8mm, the aromatization reactor and catalyst regenerator are both fixed bed reactors or moving bed reactors; when using a catalyst with a particle size of 0.05-0.5mm , its aromatization reactor and catalyst regenerator are both fluidized bed reactors.

In the present invention, in the reactor described in claims 1 and 4, the process conditions for using the gas raw material described in claim 2 and the catalyst described in claim 3 to carry out the aromatization reaction: the temperature is 400-700 ° C, the pressure 0.1-2.0MPa, the space velocity of the gas on the catalyst is 300-6000ml/gcat/h.

In order to realize the aromatization reaction, the present invention also provides a method for providing energy for the aromatization reactor described in claim 4 . The heating medium is a high-temperature gas whose temperature is 100-200°C higher than the aromatization reaction temperature, including but not limited to flue gas (containing CO, CO ₂ , H ₂ or CH ₄ , or H ₂ O, without sulfur), inert gas ( Nitrogen, argon or helium), the heat supply method is: indirect heat supply through the heat exchange tube of the aromatization fluidized bed reactor.

Due to the high reaction temperature, catalyst deactivation is inevitable, and the present invention also provides a method for regenerating the catalyst as claimed in claim 3 in the catalyst regeneration reactor as claimed in claim 4 . The regeneration temperature is 350-750° C., the pressure is 0.1-2.0 MPa, and the gas used is an inert gas with an oxygen content of 0.1%-20% (such as nitrogen, argon, helium, etc.).

The present invention also provides a method for withdrawing energy from the catalyst regeneration reactor as claimed in claim 4 . The heat exchange medium is a low temperature medium with a temperature of 200-450°C, including but not limited to flue gas (containing CO, CO ₂ , H ₂ or CH ₄ , or H ₂ O, sulfur content < 100mg/kg), inert gas (containing nitrogen, argon or helium), water vapor or pressurized saturated water or solvent oil. The heat removal method is: indirect heat exchange through the heat exchange tube of the catalyst regeneration reactor 2 .

In order to control the temperature in the catalyst regeneration reactor more effectively, in addition to the above method of withdrawing energy, the present invention also provides a method for controlling the temperature of the catalyst regeneration reactor described in claim 4 . First pass into the heat exchange medium as claimed in claim 8 in the heat exchange tube of catalyst regeneration reactor, when the temperature in the catalyst regeneration reactor is suitable for catalyst regeneration requirement, control the containing as claimed in claim 7 instead The flow rate of oxygen gas can be adjusted to achieve the purpose of controlling the temperature of the catalyst regeneration reactor. The specific method is that when the temperature increases, the feed rate of the oxygen-containing gas according to claim 7 is reduced; if the temperature decreases, the feed rate of the oxygen-containing gas according to claim 7 is increased. This can not only effectively regenerate the catalyst, but also effectively protect the catalyst from high temperature damage.

At the same time, in order to realize the circular continuous operation of aromatization reaction and catalyst regeneration as soon as possible, the present invention also provides a method for judging the end point of catalyst regeneration as claimed in claim 8 . Using the method described in claim 8, in the later stage of catalyst regeneration, if the continuous increase of the flow rate of the oxygen-containing gas described in claim 9 cannot maintain the temperature of the catalyst regeneration reactor, the catalyst regeneration reaction is considered to be basically completed. Supplemented by the _CO2 content (close to zero, and always constant) or oxygen content (close to the concentration of oxygen-containing feed gas, and always constant) in the exhaust gas at the outlet of the catalyst regeneration reactor to judge or measure the content by catalyst sampling Carbon content is judged.

Simultaneously, considering that the above-mentioned reaction and catalyst regeneration can be carried out in different reactors, the present invention also provides

Continuous operation method for different reactors.

When using the fluidized bed reactor as described in claim 4 to carry out aromatization reaction and catalyst regeneration, its continuous operation method is: at first the catalyst described in claim 3 is loaded into the aromatization reaction described in claim 1 In the fluidized bed reactor 1, feed the gas as claimed in claim 2, operate under the temperature and pressure and space velocity described in claim 4, when the activity of the catalyst is reduced to 90-95% of its highest active point , is about to part (1/5-1/10 of total catalyst amount) or whole catalyst in the aromatizing fluidized bed reactor 1 is transported in the catalyst regeneration fluidized bed reactor 2 described in claim 5 through pipeline 3 , first sweep away the aromatics or other hydrocarbon gases adsorbed on the catalyst. Then, under the temperature and atmosphere as described in claim 7, the carbon deposit on the catalyst is burned and removed. After meeting the requirements as claimed in claim 10, after the oxygen adsorbed on the catalyst is purged, it is quickly transported back to the aromatization fluidized bed reactor 1 through the pipeline 4. Then repeating this process, the catalyst in the aromatizing fluidized bed 1 can be regenerated, so that good catalytic activity can be maintained all the time, and continuous and stable operation can be performed.

When using the fixed-bed reactor as described in claim 4 to carry out aromatization reaction and catalyst regeneration, its continuous operation method is: at first the catalyst described in claim 3 is loaded into the aromatization fixed-bed reactor described in claim 1 In the bed reactor, feed the gas as claimed in claim 2, and operate under the temperature, pressure and space velocity as claimed in claim 4. When the activity of the catalyst in the aromatization fixed-bed reactor 1 was reduced to 85-90% of its highest activity point, the aromatization fixed-bed reactor 2 was opened in the same way, and the aromatization fixed-bed reactor 1 The gas is switched to aromatization fixed-bed reactor 2 for aromatization reaction. At the same time, the aromatic hydrocarbons or other hydrocarbon gases adsorbed on the catalyst in the fixed bed reactor 1 are purged clean, and used as a catalyst regeneration reactor. Under the temperature and atmosphere as claimed in claim 7, the carbon deposit on the catalyst is burned and removed, and after reaching the requirement as claimed in claim 10, after the oxygen adsorbed on the catalyst is purged, the carbon deposit as claimed in claim 2 is passed through The gas is re-aromatized. When the catalyst in the aromatization fixed-bed reactor 2 is deactivated, the catalyst in the aromatization fixed-bed reactor 2 is regenerated by the same method. By repeating the above process, the catalyst in one of the above two fixed-bed reactors can be kept with good catalytic activity at any time, while the catalyst in the other fixed-bed reactor can be regenerated. In this way, fixed bed reactor for continuous and stable operation.

When using the moving bed reactor as described in claim 4 to carry out aromatization reaction and catalyst regeneration, its continuous operation method is: at first the catalyst described in claim 3 is loaded into the aromatization reaction described in claim 1 In the moving bed reactor 1, feed the gas as claimed in claim 2, operate under the temperature and pressure and space velocity described in claim 4. When the activity of the catalyst is reduced to 85-90% of its highest active point, The first deactivated catalyst (about 1/5-1/3 of the total amount of catalyst) in the aromatization moving bed reactor 1 is removed from the aromatization moving bed reactor 1 through pipeline and device 3, and transferred to Catalyst regeneration In the moving bed reactor 2, the aromatic hydrocarbons or other hydrocarbon gases adsorbed on the catalyst are first purged away. Then, under the temperature and atmosphere as described in claim 7, the carbon deposit on the catalyst is burned and removed. After meeting the requirements as claimed in claim 10, after the oxygen adsorbed on the catalyst is purged, it is quickly loaded into the top of the aromatization moving bed reactor 1 through the pipeline and the device 4 . Then repeating this process, the catalyst in the aromatization moving bed reactor 1 can be continuously moved and regenerated, and good catalytic activity can always be maintained for continuous operation.

Compared with the currently existing methanol aromatization process, the method and device for aromatizing dimethyl ether in the present invention have the following beneficial effects.

1. Dimethyl ether can be prepared by dehydration of methanol aromatization, and then separated from water to obtain pure product. In the aromatization reactor, the by-product water per mole of aromatics is generated, which is higher than that of the direct methyl ether aromatization process 30-50% lower. This process is equivalent to separating part of the water in advance, thereby reducing the chance of the aromatization catalyst contacting water, and can increase the life of the catalyst at high temperature by 1-3 times.

2. In the process of first dehydrating dimethyl ether from methanol and then aromatizing it, a dehydrating agent is used first, and then an aromatization catalyst is used, so that the consumption of the aromatization catalyst is reduced by 30%. Due to the reduction of water adsorbed on the catalyst and the increase of acidity during the aromatization of dimethyl ether, the yield of aromatics can be 5-15% higher than that of methanol aromatization. At the same time, the gas purging time in the catalyst regeneration reactor can be shortened, and the regeneration temperature can be appropriately increased by 20° C., so that the regenerated catalyst can increase the heat brought back by the aromatization reaction by 5%. The reduction of the water pressure in the process also reduces the size of the aromatization reactor by 20%, and reduces the cost of the aromatization reactor.

3. DME is in a gaseous state, and its solubility in water is lower than that of methanol, which can reduce the complexity of subsequent separation from water.

4. Use a fluidized bed reactor and feed with methanol. If the degree of superheating is not enough, part of the liquid will make the small particle size catalyst in the fluidized bed easy to harden or difficult to fluidize. However, dimethyl ether is a gaseous raw material, which can effectively avoid this shortcoming and make the operation of the fluidized bed more stable and easier.

Description of drawings

Figure 1 is a schematic diagram of the device for continuous aromatization and catalyst regeneration provided by the present invention (both the aromatization reactor and the catalyst regenerator are fluidized beds). 1. Aromatization fluidized bed reactor (1a, gas inlet, 1b, gas outlet; 1c deactivated catalyst outlet; 1d. Fresh catalyst or regenerated catalyst inlet); 2. Catalyst regeneration fluidized bed reactor (2a , gas inlet, 2b, gas outlet; 2c regenerated catalyst outlet; 2d. deactivated catalyst inlet); 3. transport deactivated catalyst from aromatization fluidized bed reactor 1 to catalyst regeneration fluidized bed reactor 2 Pipeline; 4. A pipeline for transporting the regenerated catalyst from the catalyst regeneration fluidized bed reactor 2 to the aromatization fluidized bed reactor 1 .

Fig. 2 is a schematic diagram of the device for continuous aromatization and catalyst regeneration provided by the present invention (both the aromatization reactor and the catalyst regenerator are fixed beds). 1. Aromatization fixed-bed reactor (also used as a reactor for in-situ catalyst regeneration); 2. Aromatization fixed-bed reactor (also used as a reactor for in-situ catalyst regeneration).

Fig. 3 is a schematic diagram of the device for continuous aromatization and catalyst regeneration provided by the present invention (both the aromatization reactor and the catalyst regenerator are moving beds). 1. Aromatization moving bed reactor (1a, gas inlet, 1b, gas outlet; 1c deactivated catalyst outlet; 1d. Fresh catalyst or regenerated catalyst inlet); 2. Catalyst regeneration moving bed reactor (2a, gas Inlet, 2b, gas outlet; 2c catalyst outlet after regeneration; 2d. deactivated catalyst inlet); 3. pipeline and device for transporting deactivated catalyst from aromatization moving bed reactor 1 to catalyst regeneration moving bed reactor 2; 4. Pipes and devices for transporting the regenerated catalyst from the catalyst regeneration moving bed reactor 2 to the aromatization moving bed reactor 1 .

Detailed ways

Using the above apparatus and method, the following examples are provided to illustrate the present invention in detail, but not to limit the scope thereof.

Example 1:

Use a metal/molecular sieve type catalyst with a particle size of 0.3mm, wherein the metal content is 1% silver, 0.5% molybdenum, 1% gallium, 0.1% ruthenium, control the 0.5nm pores in the molecular sieve to be 70%, and the molecular sieve content is 65%, The Mohs hardness of the final catalyst is controlled to be greater than 7.5. The catalyst is loaded into the aromatization fluidized bed reactor 1 shown in Fig. 1, and the temperature of the aromatization fluidized bed reactor 1 is raised to 400°C by exchanging heat with high-temperature flue gas at 600°C. Feed 100% dimethyl ether feed gas, control the space velocity of dimethyl ether to 1000ml/gcat/h, and operate the pressure to 0.1MPa. When the catalyst activity drops to 95% of its highest activity point, 1/5 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 under the anaerobic condition that ensures that the pressure of the catalyst regeneration fluidized bed reactor 2 is slightly positive pressure In reactor 2. After the transportation is completed, use 300°C water vapor to purge the aromatics on the carbon-deposited catalyst, then pass in nitrogen containing 0.5% oxygen to regenerate the catalyst, and use 200°C water vapor to exchange heat to keep the temperature at 600°C. After the catalytic agent is regenerated, nitrogen is used to replace the catalyst regenerating reactor 2 and the catalyst to an oxygen-free state, and an inert gas is used to transport the regenerated catalyst to the aromatization fluidized bed reactor 1 through pipeline 4 . Repeating the above process allows the catalyst to achieve continuous regeneration and continuous production of aromatics. Within 3000 hours of stable use of the catalyst, the single-pass average conversion rate of dimethyl ether is greater than 95%, the single-pass yield of aromatics (total carbon base of feed gas) is 70%, and the selectivity of aromatics BTX (benzene, toluene, xylene) is greater than 91.6% .

Example 2:

Use a metal/molecular sieve catalyst with a particle size of 0.05mm, in which the metal content is 1% molybdenum, 0.3% silver, and 4% chromium, and the proportion of 0.5-0.7nm pores in the molecular sieve containing silicon, aluminum and phosphorus is controlled to 90%. The molecular sieve content is 50%, and the Mohs hardness of the final catalyst is controlled to be greater than 8. The catalyst was loaded into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization fluidized bed reactor 1 was raised to 450°C by exchanging heat with high-temperature nitrogen at 580°C. Feed dimethyl ether (60%), methane (5%), CO (5%), H ₂ O (10%), H ₂ (5%) and CO ₂ (15%) mixed feed gas, control the total air Speed 2000ml/gcat/h, operating pressure 0.1MPa. When the catalyst activity drops to 92% of its highest activity point, 1/6 of the catalyst is transported to the catalyst regeneration fluidized bed through pipeline 3 under the condition of ensuring that the pressure of the catalyst regeneration fluidized bed reactor 2 is slightly positive pressure and anaerobic. In reactor 2. After the transportation is completed, use methane gas at room temperature to purge the aromatic hydrocarbons on the carbon-deposited catalyst, then replace it with nitrogen gas at room temperature to a non-reducing gas state, and then pass in nitrogen gas containing 0.1% oxygen and 5% argon, and use a solvent at 250°C Heat exchange with oil to keep the regeneration temperature at 500°C. After the regeneration of the catalyst is completed, the catalyst regeneration fluidized bed reactor 2 and the catalyst are replaced with an oxygen-free state with nitrogen, and the regenerated catalyst is removed from the catalyst by an inert gas through the delivery pipeline. The regeneration fluidized bed reactor 2 is transported to the aromatization fluidized bed reactor 1 through the pipeline 4 . Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 2500 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 98%, the single-pass yield of aromatics (the total carbon base of the mixed feed gas) is greater than 45%, and the total selectivity of BTX (benzene, toluene and xylene) in aromatics Greater than 90.8%.

Example 3:

Use a metal/molecular sieve catalyst with a particle size of 0.5mm, wherein the metal content is 5% molybdenum, 3% vanadium, 0.3% manganese, and 0.1% iridium. 95%, the molecular sieve content is 70%, and the Mohs hardness of the final catalyst is controlled to be greater than 6.5. The catalyst is loaded into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization fluidized bed reactor 1 is raised to 550°C by exchanging heat with a high-temperature flue gas of 700°C. Dimethyl ether (50%), ethylene (3%), ethane (5%), propane (12%), H ₂ (4%), propylene (8%), butene (3%), butane The feed gas is mixed with alkanes (5%) and CO ₂ (10%), the total space velocity is controlled to 4000ml/gcat/h, and the operating pressure is 0.1MPa. When the catalyst activity drops to 94% of its highest activity point, the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be a slight positive pressure and under the anaerobic state, 1/5 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 In reactor 2. After the transportation is completed, use methane gas at room temperature to purge the aromatics on the carbon-deposited catalyst, and then replace it with nitrogen at room temperature to a non-reducing gas state, and then pass in nitrogen containing 10% oxygen and 10% helium, and use a 200 ° C Heat exchange with pressurized saturated water to keep the regeneration temperature at 550°C. After the regeneration of the catalyst is completed, the catalyst regeneration fluidized bed reactor 2 and the catalyst are replaced with helium to an oxygen-free state, and the regenerated catalyst is replaced with nitrogen through the delivery pipeline. The catalyst regeneration fluidized bed reactor 2 is transported to the aromatization fluidized bed reactor 1 through the pipeline 4 . Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 3200 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 98%, the single-pass yield of aromatics (the total carbon base of the mixed feed gas) is greater than 68%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics Greater than 92%.

Example 4:

Use a metal/molecular sieve catalyst with a particle size of 0.1mm, in which the metal content is 3% molybdenum, 6% tungsten, 0.5% manganese, 0.5% ruthenium, and control the pore ratio of 0.5-0.7nm in the molecular sieve containing silicon, aluminum and phosphorus 95%, the molecular sieve content is 65%, and the Mohs hardness of the final catalyst is controlled to be greater than 5.5. The catalyst is loaded into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization fluidized bed reactor 1 is raised to 550°C by exchanging heat with a high-temperature flue gas of 700°C. Pass into dimethyl ether (70%), pentane (5%), pentene (5%), butane (10%) and butene (10%) mixed feed gas, control total space velocity 4000ml/gcat/h , the operating pressure is 0.2MPa, and the catalyst activity drops to 90% of its highest activity point. To ensure that the pressure of the catalyst regeneration fluidized bed reactor 2 is a slight positive pressure and in the absence of oxygen, 1/5 of the catalyst is transported to the catalyst fluidized bed reactor 2 through the pipeline 3 . After the transportation is completed, use room temperature methane to purge the aromatics on the carbon-deposited catalyst, then use room temperature nitrogen to replace it into a non-reducing gas state, and then pass in nitrogen containing 7% oxygen, and exchange heat with 300 ° C steam. Keep the regeneration temperature at 500°C. After the regeneration of the catalyst is completed, replace the catalyst regeneration fluidized bed reactor 2 and the catalyst into an oxygen-free state with nitrogen, and transport the regenerated catalyst from the catalyst regeneration fluidized bed reactor 2 through the pipeline 4 To the aromatization fluidized bed reactor 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. In 4200 hours when the catalyst was used stably, the average conversion rate of dimethyl ether was 98%, the single-pass yield of aromatics (dimethyl ether and pentane, pentene, butane and butene total carbon base) was greater than 70.4%, and BTX in aromatics ( Benzene, toluene, xylene) had an overall selectivity of 92.5%.

Example 5:

Use a metal/molecular sieve catalyst with a particle size of 0.15mm, wherein the metal content is 6% molybdenum, the 0.5nm pores in the molecular sieve are controlled to be 70%, the molecular sieve content is 55%, and the Mohs hardness of the final catalyst is controlled to be greater than 7. The catalyst was loaded into the aromatization fluidized bed reactor 1 as shown in Fig. 1, and the temperature of the aromatization fluidized bed reactor 1 was raised to 700°C by exchanging heat with the high-temperature flue gas of 860°C. Feed mixed feed gas of dimethyl ether (90%) and methane (10%), control methane space velocity 1500ml/gcat/h, operating pressure 0.1Mpa. When the catalyst activity drops to 95% of its highest activity point, 1/10 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 under the condition that the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be slightly positive pressure and anaerobic. In reactor 2. After the transportation is completed, use methane gas at room temperature to purge the aromatics on the carbon-deposited catalyst, then replace it with nitrogen gas at room temperature to a methane-free state, then pass in nitrogen gas containing 0.5% oxygen, and exchange heat with argon gas at 300 ° C to regenerate The temperature is kept at 750°C. After the catalytic agent is regenerated, the catalyst regenerating fluidized bed reactor 2 and the catalyst are replaced with anaerobic state with nitrogen, and the regenerated catalyst is transported from the catalyst regenerating fluidized bed reactor 2 through the pipeline 4. To the aromatization fluidized bed reactor 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 4000 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is greater than 99%, the conversion rate of methane is greater than 20%, the single-pass yield of aromatics (the total carbon base of dimethyl ether and methane) is greater than 68%, and BTX (benzene, Toluene, xylene) had an overall selectivity of 93.4%.

Embodiment 6:

Use a metal/molecular sieve catalyst with a particle size of 0.25mm, in which the metal content is 1% silver, and the proportion of pores of 0.5-0.6nm in the molecular sieve containing silicon, aluminum and phosphorus is controlled to be 90%, and the molecular sieve content is 60%. The Mohs hardness of the catalyst is greater than 6.8. The catalyst was loaded into the aromatization fluidized bed reactor 1 shown in Fig. 1, and the temperature of the aromatization fluidized bed reactor 1 was raised to 450°C by exchanging heat with high-temperature flue gas at 570°C. Feed gas mixed with dimethyl ether (80%), methanol (19%) and H ₂ O (1%), control the total space velocity to 4000ml/gcat/h, and the operating pressure to 2Mpa. When the catalyst activity drops to 91% of its highest activity point, 1/7 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 under the condition that the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be slightly positive pressure and anaerobic. In reactor 2. After the transportation is completed, use methane gas at room temperature to purge the aromatic hydrocarbons on the carbon-deposited catalyst, then replace it with nitrogen gas at room temperature into a non-reducing gas state, and then pass in nitrogen gas containing 2% oxygen and 10% argon. Heat exchange with solvent oil to keep the regeneration temperature at 400°C for 6 hours. After the regeneration of the catalyst is completed, replace the catalyst regeneration fluidized bed reactor 2 and the catalyst into an oxygen-free state with nitrogen, and remove the regenerated catalyst from the catalyst regeneration flow. The fluidized bed reactor 2 is transported to the aromatization fluidized bed reactor 1 through a pipeline 4 . Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 5200 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 98%, the conversion rate of methanol is 100%, the single-pass yield of aromatics (mixed raw material gas carbon base) is greater than 67%, BTX (benzene, toluene, xylene) in aromatics The overall selectivity is greater than 93%.

Embodiment 7:

Use a metal/molecular sieve type catalyst with a particle size of 0.4mm, in which the metal content is 5% zinc, control the proportion of pores of 0.5-0.6nm in the molecular sieve containing phosphorus, silicon, and aluminum to be 100%, and the molecular sieve content is 65%, control the final The Mohs hardness of the catalyst is greater than 6.5. The catalyst was charged into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization fluidized bed reactor was raised to 480°C by exchanging heat with a high temperature flue gas of 600°C. The raw material gas of dimethyl ether (100%) is introduced, the total space velocity is controlled to 2000ml/gcat/h, and the operating pressure is 1MPa. When the catalyst activity drops to 93% of its highest activity point, the catalyst regeneration fluidized bed reactor 2 is guaranteed to have a slightly positive pressure and anaerobic state, and 1/6 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 In reactor 2. After the transportation is completed, use room temperature nitrogen to purge the aromatics on the carbon-deposited catalyst, then use room temperature nitrogen to replace it into a non-reducing gas state, then pass in nitrogen containing 7% oxygen, and use 300 ° C steam for heat exchange, so that The regeneration temperature was maintained at 350°C. After the catalyst regeneration is completed, the catalyst regeneration fluidized bed reactor 2 and the catalyst are replaced with anaerobic state with nitrogen, and the regenerated catalyst is transported from the catalyst regeneration fluidized bed reactor 2 to the aromatization fluidized bed reaction via pipeline 4 device 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 5800 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 97.2%, the per-pass yield of aromatics is greater than 64%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics is greater than 90.8%.

Embodiment 8:

Use a metal/molecular sieve type catalyst with a particle size of 0.15mm, in which the metal content is 0.5% silver, 3% zinc, and the proportion of pores in the molecular sieve containing silicon and aluminum is 90%, and the molecular sieve content is 70%. The Mohs hardness of the final catalyst is controlled to be greater than 6.5. The catalyst is loaded into the aromatization fluidized bed reactor 1 shown in Fig. 1, and the temperature of the aromatization fluidized bed reactor 1 is raised to 450°C by exchanging heat with high-temperature flue gas at 600°C. Feed gas of dimethyl ether (100%), control the total space velocity to 3000ml/gcat/h, and operate the pressure to 0.1MPa. When the catalyst activity drops to 95% of its highest activity point, 1/9 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 under the condition that the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be slightly positive pressure and anaerobic. Reactor 2. After the transportation is completed, use room temperature nitrogen to purge the aromatic hydrocarbons on the carbon deposit catalyst, then use room temperature nitrogen to replace it into a non-reducing gas state, then pass in argon containing 4% oxygen, and exchange heat with solvent oil at 250°C. The regeneration temperature was maintained at 350°C. After the catalyst is regenerated, use argon to replace the catalyst regeneration fluidized bed reactor 2 and the catalyst into an oxygen-free state, and transport the regenerated catalyst from the catalyst regeneration fluidized bed reactor 2 to the aromatization fluidized bed through the pipeline 4 In Reactor 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 4800 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 97.5%, the single-pass yield of aromatics (dimethyl ether carbon base) is greater than 70.2%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics is greater than 91.7 %.

Embodiment 9:

Use a metal/molecular sieve catalyst with a particle size of 0.25mm, in which the metal content is 5% silver, control silicon, and the ratio of pores of 0.5-0.6nm in the molecular sieve of aluminum is 100%, and the molecular sieve content is 68%, control the final catalyst. The Mohs hardness is greater than 6.3. The catalyst was loaded into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization fluidized bed reactor 1 was raised to 480°C by exchanging heat with high-temperature nitrogen at 600°C. Feed dimethyl ether (50%), raw material gas of methanol (50%), control total space velocity 6000ml/gcat/h, operating pressure 1MPa. When the catalyst activity drops to 95% of its highest activity point, the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be a slight positive pressure and in an oxygen-free state, and 1/8 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 Reactor 2. After the transportation is completed, use room temperature nitrogen to purge the aromatics on the carbon-deposited catalyst, then use room temperature nitrogen to replace it into a non-reducing gas state, then pass in nitrogen containing 2% oxygen, and exchange heat with 260 ° C steam to make The regeneration temperature was maintained at 360°C. After the catalyst regeneration is completed, the catalyst regeneration reaction fluidized bed reactor 2 and the catalyst are replaced with anaerobic state with nitrogen, and the regenerated catalyst is transported from the catalyst regeneration fluidized bed reactor 2 to the aromatization fluidized bed through the pipeline 4 In Reactor 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. In 4000 hours when the catalyst is used stably, the average conversion rate of dimethyl ether is greater than 97.5%, the conversion rate of methanol is 100%, the single-pass yield of aromatics (mixed raw material gas carbon base) is greater than 69%, BTX (benzene, toluene, xylene) had an overall selectivity greater than 89%.

Example 10:

Use a metal/molecular sieve catalyst with a particle size of 0.08mm, in which the metal content is 0.3% copper, 3% zinc and 0.2% molybdenum, and control the ratio of 0.5-0.6nm pores in the molecular sieve containing silicon, aluminum and phosphorus to 90%, The molecular sieve content is 60%, and the Mohs hardness of the final catalyst is controlled to be greater than 7. The catalyst is loaded into the aromatization fluidized bed reactor 1 shown in Figure 1, and the temperature of the aromatization reactor 1 is raised to 500°C by exchanging heat with a high-temperature flue gas of 600°C. The raw material gas of dimethyl ether (95%) and H ₂ O (5%) is introduced, the total space velocity is controlled to 4000ml/gcat/h, and the operating pressure is 0.5MPa. When the catalyst activity drops to 95% of its highest activity point, the pressure of the catalyst regeneration fluidized bed reactor 2 is guaranteed to be a slight positive pressure, and under anaerobic conditions, 1/7 of the catalyst is transported to the catalyst regeneration fluidized bed through the pipeline 3 In reactor 2. After the transportation is completed, use room temperature nitrogen to purge the aromatics on the carbon deposit catalyst, then use room temperature nitrogen to replace it into a non-reducing gas state, then pass in air, and use 300°C water vapor to exchange heat to keep the regeneration temperature at 400°C ℃. After the catalyst regeneration is completed, the catalyst regeneration fluidized bed reactor 2 and the catalyst are replaced with anaerobic state with nitrogen, and the regenerated catalyst is transported from the catalyst regeneration fluidized bed reactor 2 to the aromatization fluidized bed reaction via pipeline 4 device 1. Repeating the above process makes the catalyst continuously regenerated and aromatics are obtained continuously. Within 4200 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 96.5%, the single-pass yield of aromatics (dimethyl ether carbon group) is greater than 65%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics is greater than 92.5 %.

Example 11:

Use a metal/molecular sieve type catalyst with a particle size of 8mm, in which the metal content is 1.2% molybdenum, 5% zinc, 1% tungsten, control silicon, and the 0.5nm pores in the molecular sieve of aluminum are 50%, and the molecular sieve content is 70%, Control the Mohs hardness of the final catalyst to be greater than 5. The catalyst is loaded into aromatization fixed-bed reactor 1 as shown in FIG. 2 . The temperature of aromatization fixed-bed reactor 1 was raised to 500°C by exchanging heat with high-temperature argon at 700°C. A mixed feed gas of dimethyl ether (75%), methanol (20%) and H ₂ O (5%) is introduced, the total space velocity is controlled to 4000ml/gcat/h, and the operating pressure is 0.1MPa. When the catalyst activity drops to 90% of its highest activity point, close the feed to the fixed bed reactor 1, purge the aromatics on the coke catalyst with room temperature nitrogen and replace it with a state of no reducing gas, and then feed a 5% Oxygen and argon are exchanged with steam at 350°C to keep the regeneration temperature at 400°C. At the same time, the raw material gas is passed into the fixed-bed reactor 2 by the same method and process conditions as the above-mentioned fixed-bed reactor 1 to carry out the aromatization reaction. After the regeneration of the catalyst in the fixed-bed reactor 1 is completed, the fixed-bed reactor 1 and the catalyst are replaced with argon to an oxygen-free state, and the aromatization reaction is carried out again according to the above conditions. When the catalyst activity in fixed bed reactor 2 drops to 90% of the highest active point, repeat the same catalyst regeneration process as in fixed bed reactor 1. By switching between two fixed bed reactors, so that in any period of time The catalysts are continuously regenerated to continuously obtain aromatics. Within 37,000 hours of stable use of the catalyst, the average conversion rate of dimethyl ether and methanol is greater than 95%, the single-pass yield of aromatics (the total carbon base of dimethyl ether and methanol) is greater than 65%, and BTX (benzene, toluene, di Toluene) had an overall selectivity greater than 93.6%.

Example 12:

Use a metal/molecular sieve type catalyst with a particle size of 3mm, wherein the metal content is 3% zinc, and the molecular sieve containing silicon and aluminum is controlled to have 80% pores of 0.5nm, and the molecular sieve content is 65%, and the Mohs hardness of the final catalyst is controlled greater than 8. The catalyst was loaded into the aromatization moving bed reactor 1 shown in Figure 3, and the temperature of the aromatization moving bed reactor 1 was raised to 450°C by exchanging heat with high-temperature flue gas at 650°C. Pass into dimethyl ether (100%), control total space velocity 6000ml/gcat/h, operating pressure 0.4MPa. When the catalyst activity drops to 85% of its highest active point during the reaction, 1/3 of the catalyst is gradually removed from the bottom of the aromatization moving bed reactor 1 and enters the catalyst regeneration moving bed reactor 2 through the pipeline and device 3. Use nitrogen at room temperature to purge the aromatics on the carbon-deposited catalyst and replace it with a non-reducing gas state, then pass in nitrogen containing 5% oxygen, exchange heat with argon at 200°C, keep the regeneration temperature at 600°C, and regenerate the catalyst After completion, the catalyst regenerating moving bed reactor 2 and the catalyst are replaced to an oxygen-free state with nitrogen, and the catalyst is loaded into the top of the aromatization moving bed reactor 1 through the pipeline and device 4 . The above process is repeated so that the catalyst is continuously regenerated and continuously circulates in the aromatization moving bed reactor 1 and the catalyst regeneration moving bed reactor 2 to continuously obtain aromatics. Within 3500 hours of stable use of the catalyst, the average conversion rate of dimethyl ether is 95%, the single-pass yield of aromatics (total carbon base of dimethyl ether) is greater than 68%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics is greater than 93%.

Example 13:

Use a metal/molecular sieve type catalyst with a particle size of 8mm, in which the metal content is 0.02% platinum 6% gallium, 0.3% nickel, 0.7% iron, control the silicon, and the 0.5nm pores in the molecular sieve of aluminum are 70%, and the molecular sieve content is 55%, controlling the Mohs hardness of the final catalyst to be greater than 7. The catalyst was loaded into the aromatization moving bed reactor 1 shown in Figure 3, and the temperature of the aromatization moving bed reactor 1 was raised to 550°C by exchanging heat with high-temperature flue gas at 700°C. Feed gas mixed with dimethyl ether (51%), CO (20%), H ₂ (10%) and CO ₂ (19%), control the total space velocity to 300ml/gcat/h, and the operating pressure to 0.5MPa. When the catalyst activity drops to 90% of its highest active point during the reaction, 1/5 of the catalyst is gradually removed from the lower part of the aromatization moving bed reactor 1 and enters the catalyst regeneration moving bed reactor 2 through the pipeline and device 3, Use nitrogen at room temperature to purge the aromatics on the carbon-deposited catalyst and replace it with a non-reducing gas state, then pass in nitrogen containing 15% oxygen, exchange heat with nitrogen at 200°C, keep the regeneration temperature at 500°C, and the catalyst regeneration is complete Afterwards, nitrogen gas is used to replace the catalyst regeneration moving bed reactor 2 and the catalyst into an oxygen-free state, and the catalyst is loaded into the top of the aromatization moving bed reactor 1 through the pipeline and device 4 . The above process is repeated so that the catalyst is continuously regenerated and continuously circulates in the aromatization moving bed reactor 1 and the catalyst regeneration moving bed reactor 2 to continuously obtain aromatics. In 4000 hours when the catalyst is used stably, the average conversion rate of dimethyl ether is 94.5%, the single-pass yield of aromatics (total carbon base of dimethyl ether) is greater than 70%, and the total selectivity of BTX (benzene, toluene, xylene) in aromatics is greater than 93.8%.

Example 14:

Use a metal/molecular sieve catalyst with a particle size of 3mm, wherein the metal content is 3% silver, control the silicon, and the 0.5nm pores in the aluminum molecular sieve are 60%, and the molecular sieve content is 90%, and the Mohs hardness of the final catalyst is controlled to be greater than 6.5. The catalyst is loaded into aromatization fixed-bed reactor 1 as shown in FIG. 2 . The temperature of the aromatization fixed-bed reactor 1 was raised to 475°C by exchanging heat with high-temperature nitrogen at 700°C. Pass into dimethyl ether (65%), the mixed raw material gas of methanol (35%), control total space velocity 6000ml/gcat/h, operating pressure 0.3MPa. When the catalyst activity drops to 85% of its highest activity point, close the feed of the fixed-bed reactor 1, use room temperature nitrogen to purge the aromatics on the coke catalyst and replace it with a state without reducing gases, and then feed a 10% Oxygen and argon are exchanged with steam at 350°C to keep the regeneration temperature at 600°C. At the same time, the raw material gas is passed into the fixed-bed reactor 2 by the same method and process conditions as the above-mentioned fixed-bed reactor 1 to carry out the aromatization reaction. After the regeneration of the catalyst in the fixed-bed reactor 1 is completed, the fixed-bed reactor 1 and the catalyst are replaced with an oxygen-free state with nitrogen, and the aromatization reaction is carried out again according to the above conditions. After the catalyst activity in fixed bed reactor 2 drops to 85% of the highest active point, repeat the same catalyst regeneration process as in fixed bed reactor 1. By switching between two fixed bed reactors, so that in any period of time The catalysts are continuously regenerated to continuously obtain aromatics. Within 3000 hours of stable use of the catalyst, the average conversion rate of dimethyl ether and methanol is greater than 97%, the single-pass yield of aromatics (the total carbon base of dimethyl ether and methanol) is greater than 68%, and BTX (benzene, toluene, di Toluene) had an overall selectivity greater than 94%.

Claims (13)

1. The method for continuous aromatization of dimethyl ether is characterized in that the gas containing dimethyl ether is passed into a reactor equipped with a metal and molecular sieve composite catalyst, and aromatics are generated under temperature and pressure, and after catalyst deactivation Regenerate in situ by atmosphere replacement or move the catalyst to a catalyst regeneration reactor for regeneration, then return to the aromatization reactor, repeat the above process, and continuously prepare aromatics. 2. according to the method for the described dimethyl ether continuous aromatization of claim 1, it is characterized in that, the gas raw material of described dimethyl ether is pure dimethyl ether or dimethyl ether and other components (methanol, water, C1- A mixture of C5 hydrocarbons, CO, CO2, H2), these components can exist independently or simultaneously, and the total mass fraction of these components is not more than 50%. 3. according to the method for the described dimethyl ether continuous aromatization of claim 1, it is characterized in that, described catalyst structure is the complex of metal, molecular sieve, structural stabilizer or reinforcing agent; The kind of metal comprises zinc, silver, molybdenum , copper, nickel, manganese, chromium, platinum, iron, ruthenium, tungsten, vanadium, osmium; the metal loaded on the molecular sieve can be a single component or a composite of two or more metals; the total amount of metal The loading amount is 0.5%-10% of the total mass of the catalyst; the skeleton components of the molecular sieve are silicon, aluminum, phosphorus, and the proportion of pores with a pore size of 0.5-0.7nm in the molecular sieve is greater than 50%; the molecular sieve accounts for 50%-70% of the overall weight of the catalyst %, the others are structural stabilizers and reinforcing agents, and the Mohs hardness of the catalyst used is greater than 5; the average particle diameter of the catalyst particles is 0.05-0.5mm and 3-8mm. 4. A reactor as claimed in claim 1, comprising an aromatization reactor and a catalyst regeneration reactor, characterized in that, when using a particle diameter of 3-8mm catalyst, its aromatization reactor , catalyst regenerators are fixed bed reactors or moving bed reactors; when catalysts with a particle size of 0.05-0.5mm are used, the aromatization reactor and catalyst regenerator are both fluidized bed reactors. 5. In the reactor described in claim 1 and 4, utilize the gas raw material described in claim 2 and the catalyzer described in claim 3 to carry out the technological condition of aromatization reaction: temperature is 400-700 ℃, The pressure is 0.1-2.0MPa, and the space velocity of the gas on the catalyst is 300-6000ml/gcat/h. 6. A method for providing energy to the aromatization reactor described in claim 4, the heating medium is a high-temperature gas, and the temperature is 100-200° C. higher than the aromatization reaction temperature, including but not limited to flue gas (containing CO, CO2, H2 or CH4, or H2O, without sulfur), inert gas (including nitrogen, argon or helium), the heat supply method is: indirect heat supply through the heat exchange tube of the aromatization fluidized bed reactor. 7. A method for regenerating the catalyst according to claim 3 in the catalyst regeneration reactor as claimed in claim 4, the regeneration temperature is 350-750°C, the pressure is 0.1-2.0MPa, and the gas used is containing An inert gas with an oxygen content of 0.1%-20% (such as nitrogen, argon, helium, etc.). 8. A method for withdrawing energy from the catalyst regeneration reactor as claimed in claim 4, the heat exchange medium is a low-temperature medium, and the temperature is 200-450°C, including but not limited to flue gas (containing CO, CO2, H2 or CH4, or H2O, sulfur content <100mg/kg), inert gas (containing nitrogen, argon or helium), water vapor or pressurized saturated water or solvent oil, the heat removal method is: through catalyst regeneration reactor 2 The heat exchange tube indirect heat exchange. 9. A method for controlling the temperature of the catalyst regeneration reactor as claimed in claim 4, at first passing into the heat exchange medium as claimed in claim 8 in the heat exchange tube of the catalyst regeneration reactor, when in the catalyst regeneration reactor When the temperature is suitable for the catalyst regeneration requirements, the flow rate of the oxygen-containing gas as claimed in claim 7 should be controlled instead, and the purpose of controlling the temperature of the catalyst regeneration reactor can be achieved by adjusting the flow rate. The specific method is that when the temperature rises, the right The feeding amount of the oxygen-containing gas described in claim 7; if the temperature decreases, then increase the feeding amount of the oxygen-containing gas as described in claim 7. 10. A method for judging the end point of catalyst regeneration as claimed in claim 8, utilizing the method described in claim 8, in the later stage of catalyst regeneration, as continuously increasing the flow rate of the oxygen-containing gas described in claim 9, the catalyst cannot be maintained The temperature of the regeneration reactor depends on the completion of the catalyst regeneration reaction, supplemented by the CO2 content (close to zero and always unchanged) or the oxygen content (close to the concentration of the oxygen-containing feed gas) in the tail gas of the catalyst regeneration reactor. , and remains unchanged) to judge or to judge by measuring the carbon content of catalyst samples. 11. A continuous operation method suitable for the fluidized bed reactor described in claim 4: at first the catalyst described in claim 3 is loaded in the aromaticization fluidized bed reactor 1 described in claim 1 , feed the gas as claimed in claim 2, operate under the temperature and pressure and space velocity described in claim 4, when the activity of catalyst is reduced to 90-95% of its highest active point, be about to aromatization fluidization Part (1/5-1/10 of total catalyst amount) or whole catalyst in the bed reactor 1 is transferred in the catalyst regeneration fluidized bed reactor 2 described in claim 5 through pipeline 3, at first adsorbed on the catalyst Aromatic hydrocarbons or other hydrocarbon gases are purged clean, then, under the temperature and atmosphere as described in claim 7, the carbon deposition on the catalyst is burned and removed, after reaching the requirement as described in claim 10, after the adsorption on the catalyst After the oxygen is purged, it is quickly transported back to the aromatization fluidized bed reactor 1 through the pipeline 4, and then repeats this process to regenerate the catalyst in the aromatization fluidized bed 1, thereby maintaining good catalytic activity all the time. Continuous stable operation is possible. 12. A continuous operation method suitable for the fixed-bed reactor described in claim 5: at first the catalyzer described in claim 3 is packed in the aromatication fixed-bed reactor described in claim 1, and feeds as claimed in claim The gas described in claim 2 operates under the temperature and pressure and space velocity described in claim 4, when the activity of the catalyst in the aromatization fixed-bed reactor 1 is reduced to 85-90% of its highest activity point, according to Open the aromatization fixed-bed reactor 2 in the same way, and switch the gas of the aromatization fixed-bed reactor 1 to the aromatization fixed-bed reactor 2 to carry out the aromatization reaction. At the same time, the gas in the fixed-bed reactor 1 The aromatic hydrocarbons or other hydrocarbon gases adsorbed on the catalyst are purged and used as a catalyst regeneration reactor, and the carbon deposits on the catalyst are burned and removed under the temperature and atmosphere as claimed in claim 7, reaching the requirements as claimed in claim 10 After requesting, after the oxygen adsorbed on the catalyst is purged clean, feed the gas as claimed in claim 2, carry out aromatization reaction again, after the catalyst in the aromatization fixed-bed reactor 2 is deactivated, according to The same method regenerates the catalyst in the aromatization fixed-bed reactor 2, repeats the above-mentioned process, and can make the catalyst in one of the above-mentioned two fixed-bed reactors maintain good catalytic activity at any time, and The catalyst in another fixed bed reactor can be regenerated. In this way, the fixed bed reactor can be used for continuous stable operation. 13. A continuous operation method suitable for the moving bed reactor described in claim 4: at first the catalyst described in claim 3 is loaded in the aromatization moving bed reactor 1 described in claim 1, through Enter gas as claimed in claim 2, operate under temperature and pressure and space velocity described in claim 4. When the activity of catalyst is reduced to 85-90% of its highest active point, be about to aromatization moving bed reactor The first deactivated catalyst at the bottom of 1 (accounting for about 1/5-1/3 of the total catalyst amount) is removed from the aromatization moving bed reactor 1, and transported to the catalyst regeneration moving bed reactor 2 through the pipeline and device 3 , first purging the aromatic hydrocarbons or other hydrocarbon gases adsorbed on the catalyst, and then burning and removing the carbon deposits on the catalyst under the temperature and atmosphere as claimed in claim 7, after reaching the requirements as described in claim 10 , after purging the oxygen adsorbed on the catalyst, put it into the top of the aromatization moving bed reactor 1 through the pipeline and device 4, and then repeat this process, the catalyst in the aromatization moving bed reactor 1 can be continuously Mobile regeneration, always maintain good catalytic activity, for continuous operation.

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