Catalyst roasting device

Abstract

The utility model discloses a catalyst roasting device, which comprises a feeding machine, a roasting furnace is arranged on one side of the feeding machine, and materials are conveyed to the inner side of the roasting furnace; a preheating furnace is arranged on one side of the roasting furnace; a hydraulic station is arranged below the roasting furnace, and a discharging machine is arranged below the preheating furnace; a cooling furnace is arranged on one side of the discharging machine; the preheating furnace is designed, so that heating carrier gas is supplemented when a catalyst is roasted by the roasting furnace, and the situation that supercooled gas enters the roasting furnace to make contact with the catalyst, and consequently the catalyst is heated unevenly is prevented; the problems that an existing ammoxidation catalyst is long in roasting period, uneven in roasting, serious in crushing, poor in wear resistance and the like are solved.

Description

Technical Field

[0001] This utility model relates to the field of catalyst processing, and in particular to a catalyst roasting apparatus. Background Technology

[0002] Aromatic nitriles such as isophthalonitrile are widely used fine chemical intermediates. Among the processes for preparing isophthalonitrile, the direct ammonia oxidation of m-xylene is the simplest and most economical, and has seen rapid development in recent years. The core technology of this process is catalyst development. There are four main systems of m-xylene ammonia oxidation catalysts: V-Cr, V-Sb, VP, and Sb-Fe. Among them, V-Cr catalysts are widely used due to their ease of industrial scale-up and good reactivity. However, V-Cr catalysts also suffer from problems such as deep oxidation, numerous side reactions, and strong ammonia decomposition capabilities, resulting in the generation of large amounts of CO, CO2, and HCN, and lower selectivity and yield of the target product, isophthalonitrile.

[0003] Currently available ammonia oxidation catalysts suffer from problems such as poor integrity, poor wear resistance, severe catalyst loss in fluidized bed reactors, and poor operational stability. The main reason for these problems lies in the uneven heating of the catalyst due to incomplete calcination during the production process. Utility Model Content

[0004] The purpose of this invention is to address the shortcomings of existing technologies by proposing a catalyst roasting device.

[0005] To achieve the above objectives, the present invention adopts the following technical solution: a catalyst calcination apparatus, comprising:

[0006] Feeder;

[0007] A roasting furnace is provided on one side of the feeder to transport the material into the inside of the roasting furnace;

[0008] A preheating furnace is provided on one side of the roasting furnace;

[0009] A hydraulic station is installed below the roasting furnace, and a discharge machine is installed below the preheating furnace.

[0010] A cooling furnace is installed on one side of the discharge machine.

[0011] As a further description of the above technical solution: the feeder moves to the inside of the roasting furnace to feed the material, and then moves out of the roasting furnace after the material is conveyed.

[0012] As a further description of the above technical solution: the preheating furnace is connected to the roasting furnace and supplies preheated carrier gas to the roasting furnace.

[0013] As a further description of the above technical solution: a flap is installed on the inner side of the roasting furnace to drive the material on the inner side to rotate.

[0014] As a further description of the above technical solution: the diameters of the feed inlet and discharge outlet of the roasting furnace are smaller than the diameter of the internal accommodating cavity of the roasting furnace.

[0015] As a further description of the above technical solution: the hydraulic station is located at the bottom of the roasting furnace on the side near the feeder, and pushes one side of the roasting furnace to rise and fall.

[0016] As a further description of the above technical solution: the discharge machine is connected to the output end of the roasting furnace to transport the high-temperature material to the cooling furnace.

[0017] As a further description of the above technical solution: the cooling furnace is equipped with a spraying mechanism to spray and cool the high-temperature materials being transported.

[0018] As a further description of the above technical solution: a water tank is provided below the cooling furnace to recover the spray liquid in the cooling furnace and transport it to the top of the cooling furnace through pipelines.

[0019] As a further description of the above technical solution: a dust removal device is provided on one side of the roasting furnace.

[0020] The above technical solution has the following advantages or beneficial effects:

[0021] By designing a preheating furnace and supplementing the roasting furnace with heating carrier gas during catalyst roasting, the problem of excessively cold gas entering the roasting furnace and coming into contact with the catalyst, thus preventing uneven heating of the catalyst, and by setting up a cooling furnace to rapidly cool down the high-temperature catalyst, the problems of long roasting cycle, uneven roasting, severe breakage, and poor wear resistance of existing ammonia oxidation catalysts have been solved. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the roasting apparatus proposed in this utility model.

[0023] Figure 2 This is a schematic diagram of the roasting apparatus proposed in this utility model;

[0024] Figure 3 This is a scanning electron microscope image of the catalyst in this invention.

[0025] Legend:

[0026] 1. Feeder; 2. Roasting furnace; 21. Dust removal device; 3. Preheating furnace; 4. Hydraulic station; 5. Discharge machine; 6. Cooling furnace; 61. Spraying mechanism; 62. Water tank. Detailed Implementation

[0027] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0028] Reference Figures 1-3 An embodiment of this utility model is provided: a catalyst roasting device, comprising: a feeder 1; a roasting furnace 2 is provided on one side of the feeder 1 to transport materials to the inside of the roasting furnace 2; a preheating furnace 3 is provided on one side of the roasting furnace 2; a hydraulic station 4 is provided below the roasting furnace 2; a discharge machine 5 is provided below the preheating furnace 3; and a cooling furnace 6 is provided on one side of the discharge machine 5.

[0029] In this embodiment, the catalyst material is added to the feeder 1, which transports the material to the calcination furnace 2 for heating. At the same time, the preheating furnace preheats the carrier gas to prevent the overly cold gas from entering the calcination furnace 2 and contacting the catalyst, which would cause uneven heating of the catalyst. After calcination, the calcination furnace 2 is tilted by the hydraulic station 4, and the material is transported to the cooling furnace 6 under the action of gravity and the discharge machine 5 to quickly cool the high-temperature catalyst. This solves the problems of long calcination cycle, uneven calcination, severe breakage, and poor wear resistance of existing ammonia oxidation catalysts.

[0030] Furthermore, refer to Figure 3 In this embodiment, the catalyst is a spherical fine powder with a diameter of about 60 μm. V2O5 and CrO3 are dissolved in water to form a solution, and then oxalic acid, boric acid and ammonium molybdate are added to form a suspension. The suspension is concentrated by distilling water to form a concentrated solution of a certain concentration. Phosphoric acid and 40% silica sol are then added for loading, and finally a black-green suspension with a solid content of 40-60% is formed. The suspension is spray-dried and shaped. The calcination conditions in the calcination furnace 2 are 300℃ for 5 hours and then 500-600℃ for 10 hours.

[0031] The feeder 1 moves to the inside of the roasting furnace 2 to feed the material, and then moves out of the roasting furnace 2 after the material is conveyed.

[0032] In this embodiment, the feeder 1 is a screw feeder, which moves towards the roasting furnace 2 during feeding. It first moves into the roasting furnace 2, then rotates to add material, and automatically moves out of the roasting furnace 2 after the material is added.

[0033] The preheating furnace 3 is connected to the roasting furnace 2, and preheated carrier gas is supplied to the roasting furnace 2.

[0034] In this embodiment, the carrier gas is a compressed gas, mainly air and nitrogen. The carrier gas is heated by a preheating furnace to make the catalyst calcined more uniformly and the reaction more complete.

[0035] A flap is installed on the inner side of the roasting furnace 2, which drives the material inside to rotate. The diameters of the feed inlet and discharge outlet of the roasting furnace 2 are smaller than the diameter of the internal cavity of the roasting furnace 2.

[0036] In this embodiment, the calcining furnace 2 is a rotary calcining furnace, which calcines the catalyst by rotation and programmed temperature control. The rotary calcining furnace rotates at a certain speed during operation, ensuring more thorough calcination of the catalyst inside. The calcining furnace 2 is equipped with a flap to more evenly rotate the material during heating. The furnace chamber of the calcining furnace 2 has a large volume, with a narrowed inlet and outlet design, and spirals at the inlet and outlet for convenient material loading and unloading.

[0037] The hydraulic station 4 is located at the bottom of the roasting furnace 2 on the side near the feeder 1, and pushes one side of the roasting furnace 2 to rise and fall.

[0038] In this embodiment, the hydraulic station 4 is used to control the lifting and lowering of the furnace body when the roasting furnace 2 discharges material. One side of the roasting furnace 2 rises to form a certain angle, making it easier to discharge material through gravity and the spiral rotation of the discharge port.

[0039] The discharge machine 5 is connected to the output end of the roasting furnace 2 to transport the high-temperature material to the cooling furnace 6.

[0040] In this embodiment, the high-temperature catalyst output from the calcination furnace 2 is assisted in being transported to the cooling furnace 6 by the discharge machine 5, which is a screw feeder.

[0041] The cooling furnace 6 is equipped with a spraying mechanism 61 to spray and cool the high-temperature materials being transported.

[0042] In this embodiment, the spraying mechanism 61 is a single or multiple nozzle, which is set above the inner wall of the cooling furnace 6 to spray and cool the high-temperature catalyst being transported. After cooling to room temperature, it is transported out for post-processing and packaging.

[0043] A water tank 62 is installed below the cooling furnace 6 to recover the spray liquid in the cooling furnace 6 and transport it to the top of the cooling furnace 6 through pipelines so that the spray liquid can be recycled.

[0044] A dust removal device 21 is provided on one side of the roasting furnace 2, which can discharge the waste gas generated in the roasting furnace 2 and maintain the air pressure inside the roasting furnace 2. The dust removal device 21 is an exhaust pipe equipped with an air pump.

[0045] The catalyst prepared in this application was loaded into a fluidized bed reactor for activity evaluation. The reaction conditions were m-xylene: ammonia: air = 1:7:36, reaction temperature 415℃, and atmospheric pressure. The evaluation results showed that the m-xylene conversion rate was 99.8% and the isophthalonitrile selectivity was 97%. This catalyst was continuously evaluated in the fluidized bed reactor for three months, and its activity did not decrease, indicating good stability and minimal risk of loss.

[0046] All standard parts used in this embodiment can be purchased from the market, and irregular parts can be customized according to the description and drawings. The specific connection methods of each part adopt conventional methods such as bolts, rivets, and welding that are mature in the prior art. The machinery, parts and equipment adopt conventional models in the prior art, which will not be described in detail here. The contents not described in detail in this specification belong to the prior art known to those skilled in the art.

[0047] Finally, it should be noted that the above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Although the present utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.

Claims

1. A catalyst calcination apparatus, characterized in that, include: Feeder (1); A roasting furnace (2) is provided on one side of the feeder (1) to transport the material to the inside of the roasting furnace (2); A preheating furnace (3) is provided on one side of the roasting furnace (2); A hydraulic station (4) is provided below the roasting furnace (2), and a discharge machine (5) is provided below the preheating furnace (3); A cooling furnace (6) is provided on one side of the discharge machine (5).

2. The calcination apparatus according to claim 1, characterized in that: The feeder (1) moves to the inside of the roasting furnace (2) to feed the material, and then moves out of the roasting furnace (2) after the material is conveyed.

3. The roasting apparatus according to claim 1, characterized in that: The preheating furnace (3) is connected to the roasting furnace (2) and supplies preheated carrier gas to the roasting furnace (2).

4. The calcination apparatus according to claim 1, characterized in that: The roasting furnace (2) is equipped with a flap inside, which drives the material inside to rotate.

5. The roasting apparatus according to claim 1, characterized in that: The diameters of the feed inlet and discharge outlet of the roasting furnace (2) are smaller than the diameter of the internal cavity of the roasting furnace (2).

6. The calcination apparatus according to claim 1, characterized in that: The hydraulic station (4) is located at the bottom of the roasting furnace (2) near the feeder (1) and pushes one side of the roasting furnace (2) to rise and fall.

7. The roasting apparatus according to claim 1, characterized in that: The discharge machine (5) is connected to the output end of the roasting furnace (2) to transport the high-temperature material to the cooling furnace (6).

8. The roasting apparatus according to claim 1, characterized in that: The cooling furnace (6) is equipped with a spraying mechanism (61) to spray and cool the high-temperature materials being transported.

9. The roasting apparatus according to claim 1, characterized in that: A water tank (62) is provided below the cooling furnace (6) to recover the spray liquid in the cooling furnace (6) and transport it to the top of the cooling furnace (6) through pipeline.

10. The roasting apparatus according to claim 1, characterized in that: A dust removal device (21) is provided on one side of the roasting furnace (2).

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