Cracking reactor and cracking method and device for chemical production solid waste

Abstract

The invention relates to the technical field of chemical engineering, and discloses a cracking reactor and a cracking method and device for chemical production solid waste, the cracking reactor comprises: at least three cracking chambers which are distributed in the cracking reactor at intervals along the vertical direction, and each cracking chamber is filled with grinding balls; the rotating shaft is vertically arranged in the cracking reactor and penetrates through all the cracking chambers; the plurality of scrapers are coaxially arranged in the cracking chamber and are fixedly welded on the rotating shaft; and the plurality of partition plates are arranged between the adjacent cracking chambers along the vertical direction. The device does not need to carry out pretreatment such as crushing and drying on raw materials, the process is simple, solid waste can be fully cracked at a lower cracking temperature, and the reduction rate of the chemical residual sludge reaches up to 88.3%.

Description

Technical Field

[0001] The invention relates to the technical field of chemical industry, and in particular to a cracking reactor, a cracking method and a device for chemical production solid waste. Background Art

[0002] The residual sludge after biochemical treatment of chemical production wastewater is unstable in nature, has a high water content, and adsorbs a variety of organic and inorganic substances. With the rapid development of industrialization in recent years, the sewage treatment capacity and treatment rate have increased rapidly, resulting in a rapid increase in the production of residual sludge. Chemical residual sludge is a solid waste generated in the treatment of chemical production wastewater. The residual sludge generated after the treatment of bulk chemical production wastewater in chemical enterprises contains a large amount of toxic and harmful substances and is a hazardous waste. The state control is more stringent and the treatment technology is more complicated. At present, a large amount of fees need to be paid to professional companies for treatment of solid hazardous waste every year, which greatly increases the cost of water treatment. Therefore, how to treat the residual sludge of chemical enterprises with high efficiency and low cost, reduce it, make it harmless, and stabilize it, and ultimately achieve the purpose of resource utilization, reduce the environmental protection pressure of chemical enterprises, and help enterprises develop green, is a problem that needs to be solved urgently.

[0003] At present, the traditional and widely used methods for treating sludge are: use in agricultural production, landfill, incineration and landfill of ash after incineration. Since sludge contains high concentrations of heavy metals and there is a potential risk of heavy metals entering the food chain, sludge landfill treatment and use in agricultural production have been strictly restricted by the environmental protection department. The treatment cost of incineration is high. The above methods are all sludge treatment methods, and it is difficult to achieve the degree of resource utilization. The thermal cracking process can convert the high content of organic matter in sludge into three products: solid, gas and liquid. Among them, the solid biochar product can be used as a carbon-neutral fuel, adsorbent and substitute for carbon black; the generated gases are mainly carbon monoxide, methane, hydrogen and carbon dioxide, which can be used as gas fuel; liquid bio-oil products can be used as fuel, or for upgrading and refining of special chemicals. Therefore, sludge thermal cracking can achieve "turning waste into treasure" and has a good prospect for resource utilization.

[0004] At present, the commonly used biomass pyrolysis furnaces mainly include fixed bed, fluidized bed, vacuum moving bed, drainage bed, etc. They all have their own characteristics, but their common defects are that the pyrolysis temperature is high, the raw materials need to be pre-processed such as crushing and drying, the whole process is long, the cost is high, and it is easy to produce problems such as insufficient pyrolysis. Therefore, a solid waste pyrolysis treatment device is needed, which can overcome the shortcomings of the existing technology and control the cost at the same time to meet the actual use needs. Summary of the invention

[0005] The purpose of the present invention is to overcome the technical problems of high pyrolysis temperature, insufficient pyrolysis and complicated process of chemical production solid waste in the prior art, and to provide a pyrolysis reactor, a pyrolysis method and a device for chemical production solid waste.

[0006] In order to achieve the above object, the present invention provides a cleavage reactor in a first aspect, the cleavage reactor comprising:

[0007] At least three cracking chambers are spaced apart in the vertical direction inside the cracking reactor, and each cracking chamber is filled with grinding balls of different particle sizes;

[0008] A rotating shaft is vertically arranged inside the cracking reactor and passes through all the cracking chambers;

[0009] A plurality of scrapers are coaxially arranged in the cracking chamber and fixedly welded on the rotating shaft;

[0010] and a plurality of partitions arranged between adjacent cracking chambers in a vertical direction.

[0011] A second aspect of the present invention provides a method for cracking solid waste from chemical production, the method comprising cracking the solid waste in the cracking reactor described in the first aspect.

[0012] The third aspect of the present invention provides a cracking device for chemical production solid waste, the device comprising a screw feeder, a cracking reactor provided by the present invention, a gas condensation purifier, a high-temperature gas condenser, a membrane bioreactor and an integrated control device;

[0013] Preferably, the lower end of the screw feeder is connected to the cavity of the cleavage reactor, the upper end of the cleavage reactor is connected to the gas condensation purifier and the high-temperature gas condenser in sequence through pipelines, and the lower end of the high-temperature gas condenser is connected to the membrane bioreactor.

[0014] Through the above technical solution, the present invention achieves the following technical effects:

[0015] (1) The device provided by the present invention can fully crack solid waste at a relatively low cracking temperature.

[0016] (2) The device provided by the present invention does not require complicated crushing and drying of solid waste, thus simplifying the entire processing process.

[0017] (3) Different cracking chambers are provided in this device. From top to bottom, stainless steel (or zirconium oxide) balls of different particle sizes are added inside each cracking chamber. Driven by the scraper, the stainless steel (or zirconium oxide) balls continuously squeeze the materials. On the other hand, the stainless steel (or zirconium oxide) balls can act as good heat conductors to prevent the local temperature from being too high, resulting in insufficient pyrolysis. Under the joint action of the scraper and the stainless steel (or zirconium oxide) balls of different particle sizes in different cracking chambers, the materials can be broken step by step to achieve sufficient cracking treatment of the materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 This is a structural diagram of a chemical solid waste cracking device.

[0019] Figure 2 It is a cross-section view of the rotating shaft.

[0020] Figure 3 It is a cross-section view of the partition.

[0021] Description of Reference Numerals

[0022] 100 screw feeder; 200 cracking reactor; 210 shaft motor; 220 shaft; 230 cracking chamber; 240 high temperature resistant baffle; 250 scraper; 260 grinding ball (stainless steel or zirconia ball); 270 shaft support point; 280 slag outlet; 290 temperature monitor; 211 support frame; 212 insulation cotton; 213 dispersion hole; 300 gas condensation purifier; 310 condensate outlet; 320 high temperature gas condenser; 330 condensate inlet; 400 gas outlet; 500 membrane bioreactor; 600 integrated control device. DETAILED DESCRIPTION

[0023] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0024] In order to achieve the above object, the present invention provides a cleavage reactor in a first aspect, the cleavage reactor comprising:

[0025] At least three cracking chambers are spaced apart in the vertical direction inside the cracking reactor, and each cracking chamber is filled with grinding balls of different particle sizes;

[0026] A rotating shaft is vertically arranged inside the cracking reactor and passes through all the cracking chambers;

[0027] A plurality of scrapers fixed on the rotating shaft and arranged coaxially with the rotating shaft in the cracking chamber;

[0028] and a plurality of partitions arranged between adjacent cracking chambers in a vertical direction.

[0029] According to some embodiments of the present invention, 3-4 scrapers are arranged in each pyrolysis chamber on the same horizontal plane, and the angle between adjacent scrapers on the horizontal plane is 90-120 degrees.

[0030] In the present invention, the scraper can drive the grinding balls in the cracking chamber, which further squeeze the material, so that the material is broken and easier to be pyrolyzed. On the other hand, the rotation of the scraper stirs the hot air flow in the cracking chamber, which can prevent the local temperature from being too high and cause insufficient pyrolysis.

[0031] According to some embodiments of the present invention, the separator is provided with a plurality of evenly distributed dispersion holes.

[0032] According to some embodiments of the present invention, the apertures of the dispersion holes on different partitions gradually decrease from top to bottom along the vertical direction.

[0033] Preferably, from top to bottom along the vertical direction, the pore size of the dispersion holes on the partition located at the top of the cracking reactor is 10-20 mm, and the pore size of the dispersion holes on the partition located at the bottom of the cracking reactor is 500-1000 μm.

[0034] In the present invention, the inventors found that by changing the particle size of the dispersion holes on the partitions between adjacent cracking chambers, the apertures of the dispersion holes on different partitions gradually decrease from top to bottom in the vertical direction, so that the material can be fully cracked after being crushed step by step.

[0035] According to some embodiments of the present invention, the grinding balls are stainless steel balls and / or zirconia balls.

[0036] According to some embodiments of the present invention, the particle size of the grinding balls gradually decreases from top to bottom along the height direction of the cracking chamber.

[0037] According to some embodiments of the present invention, the particle size of the grinding balls gradually transitions from 25-40 mm at the highest position to 2-5 mm at the lowest position.

[0038] In the present invention, the inventors also found that the particle size of the grinding balls in different cracking chambers is different, and the particle size of the grinding balls gradually decreases from top to bottom along the height direction of the cracking chamber, so that the material can be gradually crushed. The smaller the particle size of the material, the easier it is to heat, thus being conducive to pyrolysis treatment.

[0039] In the present invention, the cracking reactor also includes a motor, a support point, and a slag discharge port, wherein the motor is sealed and connected to the upper end of the rotating shaft, the speed of the rotating shaft is adjusted by the motor, the support point is arranged at the lower end of the rotating shaft, and the slag discharge port is located at the bottom of the cracking reactor.

[0040] In the present invention, each cracking chamber in the cracking reactor is provided with a temperature sensor and a controller; the outside of the cracking reactor is provided with a heating wire and a temperature control device, which can timely control the temperature inside the cracking reactor; the outermost layer of the cracking reactor is provided with insulation cotton to prevent the temperature loss of the cracking chamber.

[0041] A second aspect of the present invention provides a method for cracking solid waste from chemical production, the method comprising cracking the solid waste in the cracking reactor described in the first aspect.

[0042] According to some embodiments of the present invention, the conditions for the cracking treatment include: a temperature of 300-900°C, a heating rate of 5-15°C / min, a motor speed of the screw feeder of 100-400r / min, and a cracking reactor shaft speed of 100-400r / min.

[0043] The third aspect of the present invention provides a cracking device for solid waste from chemical production, wherein the device comprises a screw feeder, a cracking reactor provided by the present invention, a gas condensation purifier, a high-temperature gas condenser, a membrane bioreactor and an integrated control device;

[0044] Preferably, the lower end of the screw feeder is connected to the cavity of the cleavage reactor, the upper end of the cleavage reactor is connected to the gas condensation purifier and the high-temperature gas condenser in sequence through pipelines, and the lower end of the high-temperature gas condenser is connected to the membrane bioreactor.

[0045] In the present invention, if Figure 1As shown, the cracking reactor 200 includes a shaft motor 210, a shaft 220, a high temperature resistant baffle 240, a scraper 250, a stainless steel (or zirconia) ball 260, a shaft support point 270, a slag discharge port 280 and a cracking reaction chamber 230; as shown in the gas condensation purifier 300, a condensate inlet 330 is arranged at the lower right end of the high temperature gas condenser 320, and a condensate outlet 310 is arranged at the upper left end, the condensate enters from the bottom and exits from the top, fully fills the high temperature gas condenser 320, and fully contacts with the high temperature gas to achieve the most efficient condensation effect; the device does not involve an exhaust gas treatment device, the generated gas is a combustible gas, and is discharged from the gas outlet 400, and can be used directly; the membrane bioreactor 500 is connected to the lower end pipeline of the high temperature gas condenser 320, and the liquid (tail water) condensed in the gas condensation purifier 300 enters the membrane bioreactor 500 for further treatment, and is discharged after meeting the standards.

[0046] In the present invention, the integrated control device 600 can control the temperature of the cleavage reactor 200, the speed of the shaft motor 210, the speed of the screw feeder 100, the flow rate of the condensate in the gas condensation purifier 300 and the drainage rate of the membrane bioreactor 500.

[0047] In order to describe in more detail a method for pyrolysis of chemical production solid waste provided by the present invention, Figure 1-3 The instructions are as follows:

[0048] The lower end of the screw feeder 100 is connected to the cavity of the cracking reactor 200, and a certain amount of material enters the cracking reactor 200 stably. A heating wire and a temperature control 290 device are provided outside the cracking reactor 200, which can timely control the temperature inside the cracking chamber 230; the outermost layer of the cracking reactor 200 has a heat preservation cotton 212 to prevent the temperature loss of the cracking chamber 230. A rotating shaft 220 is provided inside the cracking reactor 200, and the upper end of the rotating shaft 220 is connected to the external motor 210 by a dynamic seal bearing. The entire device is sealed and connected. The speed of the rotating shaft 220 is adjusted by the external motor 210 and controlled by the integrated control device 600. A supporting point 270 of the rotating shaft 220 is provided at the lower end of the cracking reactor 200. The rotating shaft 220 runs through all the cracking chambers 230. A scraper 250 is welded on the same horizontal plane of the rotating shaft 220 of each cracking chamber 230, and the angle of each scraper 250 on the horizontal plane is 120 degrees. From top to bottom, stainless steel (or zirconium oxide) balls 260 of different particle sizes are added inside each cracking chamber 230. Driven by the scraper 250, the materials can be squeezed continuously on the one hand, and the stainless steel (or zirconium oxide) balls 260 can act as a good heat conductor on the other hand, so that the materials are heated more evenly. A porous high-temperature resistant partition 240 (cross section as shown in FIG. 2 ) is arranged between each cracking chamber 230. Figure 3As shown in FIG. 2 , the aperture of the sieve holes on the partition 240 gradually decreases from top to bottom, so that the material is broken step by step to achieve sufficient cracking. The small amount of ultrafine biochar obtained in the lower layer is recovered by the material collection at the lower end. At the same time, each cracking chamber 230 is provided with a temperature sensor and a controller.

[0049] A gas outlet is provided at the upper end of the cracking reactor 200, and the high-temperature gas generated in the cracking reactor 200 enters the gas condensation purification device (including the gas condensation purifier 300 and the high-temperature gas condenser 320) therefrom. A portion of the non-condensable combustible gas is discharged from the side of the gas condensation purification device and collected, and the condensed liquid (tail water) enters the membrane bioreactor 500 for treatment and then is discharged in compliance with the standards.

[0050] According to a particularly preferred embodiment of the present invention, the present invention provides a method for pyrolysis of chemical solid waste. Figure 1 The cracking device shown is used, and the specific operation method includes:

[0051] The chemical excess sludge to be treated is fed into the screw feeder 100. The feeding speed is adjusted by the built-in motor 210. The rotation speed is 0-400r / min. The chemical excess sludge enters the cavity of the cleavage reactor 200 through the screw feeder 100. The cleavage reactor 200 has 3-4 cleavage chambers 230 spaced from top to bottom. Each cleavage chamber 230 is provided with 3-4 scrapers 250. The angle between adjacent scrapers 250 in the horizontal plane is 90-120 degrees. From top to bottom along the vertical direction, the apertures of the dispersion holes 213 on different partitions 240 gradually decrease. The apertures of the dispersion holes 213 on the partition 240 at the top of the cleavage reactor 200 are 10-20mm, and the apertures of the dispersion holes 213 on the partition 240 at the top of the cleavage reactor 200 are 10-20mm. The aperture of the dispersion hole 213 on the bottom partition 240 is 500-1000 μm; each cracking chamber 230 is filled with grinding balls 260, and the particle size of the grinding balls 260 gradually decreases from top to bottom along the height direction of the cracking chamber 230, and the particle size of the grinding balls 260 gradually transitions from 25-40 mm at the highest position to 2-5 mm at the lowest position; the internal temperature of the cracking reactor 200 is controlled at 300-500°C, and the heating rate is 5-15°C / min. The weight of the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is recorded, and the reduction rate of the residual sludge is calculated.

[0052] The present invention will be described in detail below through examples.

[0053] The reduction rate of excess sludge (%) = 100% × (the mass of the chemical excess sludge to be treated - the mass of the solid residue after treatment) / the mass of the chemical excess sludge to be treated.

[0054] The raw materials in the following examples are all commercially available products.

[0055] Example 1

[0056] The present invention provides a method for cracking chemical solid waste. Figure 1 The cracking device shown is used, and the specific operation method includes:

[0057] 500 kg of chemical waste sludge to be treated (water content of 77%) is directly fed into the screw feeder 100 . The feeding speed is adjusted by the built-in motor 210 , and the rotation speed is 200 r / min. The chemical waste sludge enters the cavity of the pyrolysis reactor 200 through the screw feeder 100 . Among them, the cracking reactor 200 has four cracking chambers 230 spaced from top to bottom, each cracking chamber 230 is provided with three scrapers 250, and the angle between adjacent scrapers 250 in the horizontal plane is 120 degrees. The apertures of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 are 20mm, 10mm, and 1000μm, respectively. Each cracking chamber 230 is filled with grinding balls 260, and the particle sizes of the grinding balls 260 are 40mm, 20mm, 10mm, and 5mm from top to bottom along the height direction of the cracking chamber 230. The internal temperature of the cracking reactor 200 is controlled at 400°C, the heating rate is 10°C / min, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 80kg, the reduction rate of the residual sludge is 84%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0058] Example 2

[0059] The present invention provides a method for cracking chemical solid waste. Figure 1 The cracking device shown is used, and the specific operation method includes:

[0060] 600 kg of chemical waste sludge to be treated (with a water content of 69%) is directly fed into the screw feeder 100 . The feeding speed is adjusted by the built-in motor 210 , and the rotation speed is 150 r / min. The chemical waste sludge enters the cavity of the pyrolysis reactor 200 through the screw feeder 100 . Among them, the cracking reactor 200 has four cracking chambers 230 spaced from top to bottom, each cracking chamber 230 is provided with four scrapers 250, the angles between adjacent scrapers 250 in the horizontal plane are all 90 degrees, the apertures of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 are 10mm, 5mm, and 500μm, respectively, and each cracking chamber 230 is filled with grinding balls 260, and the particle sizes of the grinding balls 260 are 25mm, 15mm, 5mm, and 2mm from top to bottom along the height direction of the cracking chamber 230, respectively. The internal temperature of the cracking reactor 200 is controlled at 500°C, the heating rate is 10°C / min, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 84kg, the reduction rate of the residual sludge is 86%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0061] Example 3

[0062] The present invention provides a method for cracking chemical solid waste. Figure 1 The cracking device shown is used, and the specific operation method includes:

[0063] 500 kg of chemical waste sludge to be treated (water content of 78%) is directly fed into the screw feeder 100 . The feeding speed is adjusted by the built-in motor 210 , and the rotation speed is 150 r / min. The chemical waste sludge enters the cavity of the pyrolysis reactor 200 through the screw feeder 100 . Among them, the cracking reactor 200 has three cracking chambers 230 spaced from top to bottom, each cracking chamber 230 is provided with three scrapers 250, the angle between adjacent scrapers 250 in the horizontal plane is 120 degrees, the apertures of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 are 15mm, 8mm, and 800μm, respectively, and each cracking chamber 230 is filled with grinding balls 260, and the particle sizes of the grinding balls 260 are 30mm, 15mm, 8mm, and 2mm from top to bottom along the height direction of the cracking chamber 230, respectively. The internal temperature of the cracking reactor 200 is controlled at 500°C, the heating rate is 10°C / min, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 73kg, the reduction rate of the residual sludge is 85.4%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0064] Example 4

[0065] According to the same method as Example 1, the difference is that the apertures of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 are 10 mm, 5 mm, and 500 μm, respectively. The solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 75 kg, the reduction rate of the remaining sludge is 85%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0066] Example 5

[0067] The same method as in Example 1 is used, except that the heating rate inside the cracking reactor 200 is 5°C / min, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 74 kg, the reduction rate of the remaining sludge is 85.2%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0068] Example 6

[0069] The same method as in Example 1 is used, except that the temperature in the cracking reactor 200 is controlled at 700°C, 68 kg of solid residue after thermal cracking is obtained from the slag discharge port 280, the reduction rate of the remaining sludge is 86.4%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0070] Example 7

[0071] The same method as in Example 2 is used, except that the internal temperature of the cracking reactor 200 is controlled at 800°C, 70 kg of solid residue after thermal cracking is obtained from the outlet of the slag discharge port 280, the reduction rate of the remaining sludge is 88.3%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0072] Example 8

[0073] The same method as in Example 1 is used, except that the internal temperature of the cracking reactor 200 is controlled at 900°C, 60 kg of solid residue after thermal cracking is obtained from the outlet of the slag discharge port 280, the reduction rate of the remaining sludge is 88%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0074] Example 9

[0075] The same method as in Example 1 is used, except that the particle sizes of the grinding balls 260 are 25 mm, 15 mm, 5 mm, and 2 mm from top to bottom along the height direction of the cracking chamber 230, respectively. The solid residue after thermal cracking obtained from the slag discharge port 280 is 73 kg, the reduction rate of the remaining sludge is 85.4%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide, and other hydrocarbon-containing gases.

[0076] Comparative Example 1

[0077] The same method as in Example 1 is used, except that the heating rate inside the cracking reactor 200 is 20°C / min, 90 kg of solid residue after thermal cracking is obtained from the outlet of the slag discharge port 280, the reduction rate of the remaining sludge is 82%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0078] Comparative Example 2

[0079] According to the same method as Example 1, except that the grinding balls 260 are not loaded in the cracking chamber 230, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 95 kg, the reduction rate of the remaining sludge is 81%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0080] Comparative Example 3

[0081] The same method as in Example 1 is used, except that the particle sizes of the grinding balls 260 are 50 mm, 30 mm, 20 mm, and 10 mm respectively from top to bottom along the height direction of the cracking chamber 230. The solid residue after thermal cracking obtained from the slag discharge port 280 is 91 kg, the reduction rate of the remaining sludge is 81.8%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide, and other hydrocarbon-containing gases.

[0082] Comparative Example 4

[0083] The same method as in Example 1 is used, except that the particle size of the grinding balls 260 in each cracking chamber 230 is 40 mm, the solid residue after thermal cracking obtained from the slag discharge port 280 is 96 kg, the reduction rate of the remaining sludge is 80.8%, and the pyrolysis gas obtained is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0084] Comparative Example 5

[0085] According to the same method as Example 1, the difference is that the apertures of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 are 30 mm, 20 mm, and 2000 μm, respectively. The solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 103 kg, the reduction rate of the remaining sludge is 79.4%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0086] Comparative Example 6

[0087] According to the same method as Example 1, except that the aperture of the dispersion holes 213 on the partition 240 between adjacent cracking chambers 230 is 5 mm, the solid residue after thermal cracking obtained from the outlet of the slag discharge port 280 is 82 kg, the reduction rate of the remaining sludge is 83.6%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0088] Comparative Example 7

[0089] The same method as in Example 1 is used, except that the motor speed of the screw feeder 100 is 450 r / min, the solid residue after thermal cracking obtained from the slag discharge port 280 is 92 kg, the reduction rate of the remaining sludge is 81.6%, and the obtained pyrolysis gas is hydrogen, methane, carbon monoxide and other hydrocarbon-containing gases.

[0090] It can be seen from the data of Examples 1-9 and Comparative Examples 1-4 that the device described in the present invention can crush the material step by step under the joint action of the scraper and the grinding balls of different particle sizes in different cracking chambers to achieve sufficient cracking treatment of the material, so that the reduction rate of chemical excess sludge is as high as 88.3%. In Comparative Example 1, the heating rate inside the cracking reactor is increased, so that the excess sludge is not fully cracked and the reduction rate of the excess sludge is reduced; in Comparative Example 2, the grinding balls are not loaded in the cracking chamber, so that the excess sludge is not fully cracked and the reduction rate of the excess sludge is further reduced; in Comparative Example 3, the particle size of the grinding balls in each cracking chamber is not within the range defined by the present invention. The particle size of the grinding balls in the lysis chambers of Comparative Example 4 is the same, which leads to insufficient lysis of the residual sludge and a decrease in the reduction rate of the residual sludge; the aperture size of the dispersion holes on the partitions between adjacent lysis chambers in Comparative Example 5 is not within the range specified by the present invention, which leads to insufficient lysis of the residual sludge and a further decrease in the reduction rate of the residual sludge; the aperture size of the dispersion holes on the partitions of the lysis chambers of Comparative Example 6 is the same, which leads to insufficient lysis of the residual sludge and a decrease in the reduction rate of the residual sludge; the motor speed is increased in Comparative Example 7, which leads to insufficient lysis of the residual sludge and a further decrease in the reduction rate of the residual sludge.

[0091] In summary, according to the method of the present invention, a plurality of different cracking chambers are arranged in the cracking reactor, and a porous partition is arranged between adjacent cracking chambers. Each cracking chamber is filled with grinding balls and scrapers of different particle sizes. Under the joint action of the scrapers and grinding balls, the solid waste is crushed step by step and the material is fully cracked.

[0092] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A cracking reactor, characterized in that: The cleavage reactor comprises: At least three cracking chambers are spaced apart in the vertical direction inside the cracking reactor, and each cracking chamber is filled with grinding balls of different particle sizes; A rotating shaft is vertically arranged inside the cracking reactor and passes through all the cracking chambers; A plurality of scrapers fixed on the rotating shaft and arranged coaxially with the rotating shaft in the cracking chamber; and a plurality of partitions arranged between adjacent cracking chambers in a vertical direction.

2. The cleavage reactor according to claim 1, wherein In each cracking chamber, 3-4 scrapers are arranged on the same horizontal plane, and the angle between adjacent scrapers on the horizontal plane is 90-120 degrees.

3. The cleavage reactor according to claim 1 or 2, wherein: The partition is provided with a plurality of evenly distributed dispersion holes.

4. The cleavage reactor according to claim 3, wherein From top to bottom along the vertical direction, the apertures of the dispersion holes on different partitions gradually decrease; Preferably, from top to bottom along the vertical direction, the aperture of the dispersion holes on the partition located at the top of the cracking reactor is 10-20 mm, and the aperture of the dispersion holes on the partition located at the bottom of the cracking reactor is 500-1000 μm.

5. The cleavage reactor according to claims 1-4, wherein: The grinding balls are stainless steel balls and / or zirconium oxide balls.

6. The cleavage reactor according to claims 1-5, wherein: The particle size of the grinding balls gradually decreases from top to bottom along the height direction of the cracking chamber.

7. The cleavage reactor according to claims 1-6, wherein: The particle size of the grinding balls gradually transitions from 25-40 mm at the highest position to 2-5 mm at the lowest position.

8. A method for pyrolysis of solid waste from chemical production, characterized in that: The method comprises subjecting solid waste to cracking treatment in a cracking reactor as described in any one of claims 1 to 7.

9. The method according to claim 8, wherein: The conditions for the cracking treatment include: a temperature of 300-900°C, a heating rate of 5-15°C / min, a motor speed of the screw feeder of 100-400r / min, and a shaft speed of the cracking reactor of 100-400r / min.

10. A cracking device for solid waste from chemical production, characterized in that: The device comprises a screw feeder, a cracking reactor according to any one of claims 1 to 7, a gas condensation purifier, a high-temperature gas condenser, a membrane bioreactor and an integrated control device. Preferably, the lower end of the screw feeder is connected to the cavity of the cleavage reactor, the upper end of the cleavage reactor is connected to the gas condensation purifier and the high-temperature gas condenser in sequence through pipelines, and the lower end of the high-temperature gas condenser is connected to the membrane bioreactor.

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