A pretreatment method and device for improving high temperature hypoxia reaction

Abstract

The present invention discloses a pretreatment method and device for improving high-temperature anoxic reaction, the method comprising pre-treating materials that need to undergo high-temperature anoxic reaction, so that the materials after pre-treatment are more in line with the expected effect of the high-temperature anoxic reaction. The pre-treatment method comprises concentration, dehydration, dissociation, drying, batching, homogenization, and molding, and the physical and chemical properties of the materials entering the high-temperature anoxic reaction are optimized after pre-treatment. In practice, different combinations of links can be selected according to the different physical and chemical properties of the materials to achieve the purpose of optimizing the physical and chemical properties of the materials, so as to achieve better high-temperature anoxic reaction effects for different materials. The present invention can make the materials to be treated use less reaction energy in the high-temperature anoxic reaction and obtain a faster reaction speed; the entire high-temperature anoxic process can be made more controllable through homogenization and molding, greatly reducing the blind spots of the high-temperature anoxic reaction and reducing the residues of harmful substances.

Description

Technical Field

[0001] The present invention belongs to the technical field of harmless treatment and resource utilization of solid waste and hazardous waste in environmental restoration, and more specifically, relates to a pretreatment method and device for improving high-temperature anoxic reaction. Background Art

[0002] With the development of human society, a lot of solid waste and hazardous waste with certain calorific value have been gradually produced. Some hazardous wastes are formed by liquid residues in harmless solids, and some solid waste and hazardous waste can be harmlessly treated or recycled through high-temperature anoxic reaction. For example, the ground sludge and tank bottom sludge formed during the mining, refining, storage and transportation of crude oil; for example, the sludge accumulated by the oxidation pond and sewage treatment system of coal gasification site for a long time; for example, a large number of waste tires generated in the automobile market; for example, a large number of low calorific value tailings generated in the production process of coal mining enterprises; for example, kitchen waste and domestic waste with certain calorific value generated in dining and daily life. At present, the market mostly uses physical and chemical sorting, solidification and stabilization, biological fermentation, incineration, pyrolysis, smoldering and other methods to treat the above solid waste and hazardous waste. Physical and chemical sorting can recover high concentrations of liquid or metal remaining in solids, but there are still a lot of liquids remaining in solids. Solidification and stabilization cannot completely achieve reduction, and the biological fermentation process is slow and not easy to control. At present, incineration, pyrolysis, smoldering and other methods are widely used to treat the above solid waste and hazardous waste, and the treatment effect is more thorough. In principle, incineration is a reaction that occurs under sufficient oxygen conditions. It mainly uses the by-product steam from high-temperature flue gas for power generation. The one-time investment and cost are relatively high, but it does not achieve true resource utilization. Pyrolysis or smoldering is an anaerobic or anoxic reaction. It mainly obtains by-product pyrolysis gas and tar in a high-temperature anoxic environment, which can achieve resource utilization to a certain extent. When pyrolysis or smoldering is used to treat sludge and oil sludge, the sludge and oil sludge can also be processed into clean soil, which has certain environmental protection significance. At present, pyrolysis and smoldering are still in the pilot or industrial trial operation stage, and have not formed large-scale commercial applications. The reason is that there is a lack of early pretreatment links, the physical and chemical properties of the overall material cannot be controlled, and the material is roughly subjected to high-temperature anoxic reaction, resulting in slow high-temperature anoxic reaction speed, uneven reaction, most of the organic volatile components are consumed, there are few reaction by-products, the harmful substances in the materials to be treated are not cleanly removed, and the exhaust gas composition is complex and unstable. Summary of the invention

[0003] In view of the problems existing in the existing high-temperature anoxic reaction, the purpose of the present invention is to provide a pretreatment method and device for improving the high-temperature anoxic reaction, so that the originally rough high-temperature anoxic reaction process can be controlled and the reaction effect is better.

[0004] To achieve the above object, the technical solution adopted by the present invention is:

[0005] A pretreatment method for improving high temperature anoxic reaction, the method is to pre-treat the material to be treated according to its physical and chemical properties to adjust the properties of the material to be treated, specifically comprising the following steps:

[0006] Step 1, concentration: if the moisture content of the material to be treated is less than 60%, directly enter step 2; if the moisture content of the material to be treated is between 60% and 99.9%, reduce the moisture content of the material to be treated to less than 60% by gravity sedimentation, centrifugation, adsorption, electrochemical enrichment, flocculation, and mechanical classification dehydration;

[0007] Step 2, dehydration: if the moisture content of the material to be treated is lower than 40%, directly proceed to step 3; if the moisture content of the material to be treated is between 40% and 60%, the moisture content of the material to be treated is reduced by positive pressure filtration, negative pressure filtration, centrifugation, mechanical classification dehydration, and chemical reaction dehydration until the moisture content is lower than 40%;

[0008] Step 3, dissociation: if the particle size of the material to be processed is less than 30mm, directly proceed to step 4; if the particle size of the material to be processed is greater than 30mm, separate or disperse the liquid or solid with calorific value in the material to be processed from the original surrounding medium by crushing, grinding and analysis, so that the particle size of the material to be processed is less than 30mm;

[0009] Step 4, drying: if the moisture content of the material to be processed is less than 20%, directly proceed to step 5; if the moisture content of the material to be processed is between 20% and 40%, the water and other volatile components in the material to be processed are taken away by low-temperature hot gas to reduce the moisture content of the material to be processed until the moisture content is less than 20%;

[0010] Step 5, batching: If the reaction potential barrier of the material to be processed is low, that is, when the temperature is below 500°C, the thermal energy RT is greater than the activation energy E a , then directly go to step 6; if the reaction potential barrier of the material to be treated is high, the temperature below 500℃ does not satisfy the requirement that the thermal energy RT is greater than the activation energy E a , then add auxiliary fuel with lower reaction potential barrier or catalyst to reduce reaction potential barrier to the material to be treated until the overall reaction potential barrier is reduced, so that the temperature below 500℃ can satisfy the requirement that thermal energy RT is greater than activation energy E a ;

[0011] Step 6, homogenization: if the homogenization degree of the material to be processed is above 60%, proceed to step 7; if the homogenization degree of the material to be processed is less than 60%, the material to be processed is mixed by a mobile mechanical mixer or a fixed mixing device to form a mixed material with a homogenization degree of more than 60% and a uniform texture;

[0012] Step 7, molding: if the porosity of the material to be processed is above 25%, it directly enters the high-temperature anoxic reaction; if the porosity of the material to be processed is lower than 25%, the material to be processed is molded by extrusion or rolling.

[0013] Furthermore, the material to be processed is a liquid or solid or a solid-liquid mixture with a calorific value greater than 1 MJ / Kg when the water content is less than 40%; the material to be processed includes oil sludge.

[0014] Furthermore, the physical and chemical properties include one or more of concentration, water content, specific surface area, porosity, degree of homogenization, calorific value, shape, chemical composition, heat capacity, and reaction potential energy barrier.

[0015] Furthermore, the high temperature is between 300°C and 1300°C.

[0016] Furthermore, the low-temperature hot gas in step 4 is one of steam, waste flue gas, air, and inert gas, and its temperature is between 100°C and 500°C.

[0017] Furthermore, in step 5, the auxiliary fuel includes pulverized coal, sawdust, and rice husk, and the catalyst includes clay and lime. The amount of the auxiliary fuel or catalyst added is 0.1% to 40%.

[0018] Furthermore, the degree of homogenization in step 6 is determined by assigning weights of 30%, 25%, 10% and 35% to the moisture content, median particle size, calorific value material content and permeability coefficient of the material, respectively.

[0019] Furthermore, the shapes of the molding in step 7 include honeycomb, columnar, pillow, spherical or irregular granular shapes.

[0020] A pretreatment device for improving high temperature anoxic reaction, comprising 7 modules: S1 concentration module, S2 dehydration module, S3 dissociation module, S4 drying module, S5 batching module, S6 homogenization module, and S7 molding module;

[0021] The S1 thickening module comprises an S11 slurry mixing tank, an S12 mud pump and an S13 thickening tank which are connected in sequence, wherein the discharge port of the S11 slurry mixing tank is connected to the feed port of the S12 mud pump, and the discharge port of the S12 mud pump is connected to the S13 thickening tank through a pipeline;

[0022] The S2 dehydration module includes an S21 filter press mud pump and an S22 filter press, wherein the S21 filter press mud pump is connected to the S22 filter press through a pipeline, and an S23 material receiving wide belt is provided under the S22 filter press for transporting the filtered material to the S3 dissociation module;

[0023] The S3 dissociation module includes an S31 blockage clearing machine and an S33 cage crusher. The S31 blockage clearing machine is arranged below the S23 material receiving wide belt. A S32 crushing pull-type belt scale is arranged between the discharge port of the S31 blockage clearing machine and the feed port of the S33 cage crusher, which is used to transport the block material to the S33 cage crusher. The discharge port of the S33 cage crusher is provided with an S34 vibrating screen, which is inclined, and an S36 under-screen belt is arranged below the screen.

[0024] The S4 drying module includes an S41 buffer bin and an S43 dryer. The S41 buffer bin is arranged below the S36 screen belt. A S42 drying pull-type belt scale is arranged between the S41 buffer bin discharge port and the S43 dryer feed port. Qualified bulk materials are weighed by the S42 drying pull-type belt scale and then transported to the S43 dryer.

[0025] The S5 batching module includes an S51 batching belt, an S52 first auxiliary silo, an S53 second auxiliary silo, and an S54 oil sludge silo; the S51 batching belt is located between the S43 dryer outlet and the S54 oil sludge silo inlet, and is used to transport the dried bulk material to the S54 oil sludge silo; the S52 first auxiliary silo and the S53 second auxiliary silo are used to add auxiliary fuel or catalyst; the S52 first auxiliary silo is connected to an S55 first auxiliary material reduction scale, the S53 second auxiliary silo is connected to an S56 second auxiliary material reduction scale, and the S54 oil sludge silo is provided with an S57 batching pull-type belt scale for quantitative batching;

[0026] The S6 homogenizing module includes an S61 strong mixing belt arranged below the S55 first auxiliary material reduction scale, the S56 second auxiliary material reduction scale and the S57 batching pull-type belt scale, and an S62 strong mixer arranged under the S61 strong mixing belt;

[0027] The S7 molding module includes an S71 molding belt, an S72 molding buffer bin, and an S74 molding machine; the S71 molding belt is located between the discharge port of the S62 intensive mixer and the feed port of the S72 molding buffer bin, and is used to transport the mixed materials to the S72 molding buffer bin; the S72 molding buffer bin is provided with an S73 molding pull-type belt scale, which is used to quantitatively feed the materials to the S74 molding machine.

[0028] Furthermore, the S3 dissociation module also includes an S35 bucket elevator, the feed port of the S35 bucket elevator is connected to the downward inclined side of the S34 vibrating screen, the discharge port of the S35 bucket elevator is connected to the S33 cage crusher, and the qualified bulk materials are transported to the S4 drying module by the S36 screen belt, and the unqualified bulk materials are returned by the S35 bucket elevator to the S33 cage crusher for further crushing.

[0029] Furthermore, the number of auxiliary material silos in the S5 batching module is 2 or more, and each of the auxiliary material silos is connected to an auxiliary material reduction scale.

[0030] The beneficial effects of the present invention are as follows: after the material to be treated is pretreated to adjust its physical and chemical properties, a high-temperature anoxic reaction is carried out:

[0031] 1) After the physical and chemical properties are adjusted by the pretreatment device, the material to be treated can achieve a faster reaction speed in the high temperature and oxygen-deficient reaction; compared with the rough feeding method, the reaction speed can be at least 4 times faster.

[0032] 2) The treatment process uses less reaction energy and can make full use of the waste heat of flue gas to dry the materials, which can indirectly save the electricity consumption of high-temperature oxygen-deficient reactions.

[0033] 3) More valuable reaction by-products are obtained from the flue gas condensate of the high-temperature anoxic reaction. By adjusting the physical and chemical properties of the material to be treated through pretreatment, the valuable volatile components can be smoothly pyrolyzed and volatilized to avoid being trapped in the material layer due to low permeability, thereby condensing and recovering more by-products in the flue gas.

[0034] 4) The materials to be processed have lower levels of harmful substances remaining. Through homogenization and molding, the entire high-temperature hypoxia process can be made more controllable, greatly reducing the blind spots of the high-temperature hypoxia reaction.

[0035] 5) Through the concentration and dehydration of materials in the early stage, the chlorine content inside the materials can be controlled, and the production of dioxins and other chlorinated organic compounds by high-temperature anoxic reactions can be reduced; the ordered porous channels formed in the pre-treated materials can avoid the combustion of excessive organic volatile components and reduce carbon emissions. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 A flow chart for determining a pretreatment method for improving the effect of high temperature and hypoxia reaction;

[0037] Figure 2 A diagram of a pretreatment device for improving the effect of high temperature and hypoxia reaction;

[0038] Among them, S11 slurry mixing tank, S12 mud pump, S13 thickening tank, S21 filter press mud pump, S22 filter press, S23 wide belt for receiving materials, S31 blockage clearing machine, S32 pull-type belt scale (crushing), S33 cage crusher, S34 vibrating screen, S35 bucket elevator, S36 under-screen belt, S41 buffer bin, S42 pull-type belt scale (drying), S43 dryer, S51 batching belt, S52 auxiliary material 1 bin, S53 auxiliary material 2 bin, S54 oil sludge bin, S55 auxiliary material 1 reduction scale, S56 auxiliary material 2 reduction scale, S57 pull-type belt scale (batch), S61 strong mixing belt, S62 strong mixer, S71 molding belt, S72 molding buffer bin, S73 pull-type belt scale (molding), S74 molding machine. DETAILED DESCRIPTION

[0039] The present invention is further described in detail below with reference to specific embodiments, but is not intended to limit the present invention.

[0040] In this embodiment, oil sludge is used as the material to be processed.

[0041] Figure 1 The paper shows a pretreatment method identification process for improving high-temperature anoxic reaction of sludge, which lists P1, P2, P4 moisture content control, P3 particle size control, P5 reaction potential barrier control, P6 homogenization degree control, P7 porosity control, and lists the corresponding links 1 concentration, 2 dehydration, 3 dissociation, 4 drying, 5 batching, 6 homogenization, and 7 molding. Figure 1 The physical and chemical properties corresponding to P1…Pn can be replaced by other physical and chemical properties, and the order and number of cycles can be adjusted according to the physical and chemical properties of the material to be processed, and the corresponding 1…n links must also change accordingly.

[0042] See also Figure 1, the material to be treated is set as sludge, the moisture content of P1 is between 60% and 99.9%, and concentration treatment is adopted. After concentration, the moisture content of P2 is between 40% and 60%, and dehydration treatment is adopted. After dehydration, the particle size of P1 is blocky, the size is greater than 30mm, and dissociation treatment is adopted. After dissociation, the moisture content is greater than 20%, and the waste heat of flue gas is fully utilized for drying to reduce the moisture content to less than 20%. In the batching stage, pulverized coal, sawdust, rice husks, and lime are added as auxiliary materials to reduce the reaction potential barrier of the overall material to reduce the high temperature and oxygen-deficient reaction time. It is determined that the homogenization degree of the material to be treated is less than 60%, and the homogenization stage is carried out. The material to be treated is mixed by a mobile mechanical mixer or a fixed mixing device to form a mixed material with a homogenization degree of more than 60% and a uniform texture. In order to control the better porosity of P7 and make the porosity above 25%, a molding stage is required, and the molding operation is controlled to become a shape with a larger specific surface area and porosity, such as honeycomb, columnar, pillow, spherical or irregular granular. Identification through pretreatment methods can provide a clearer process flow for the pretreatment process of high-temperature anoxic reaction.

[0043] Among them, the method for determining the homogenization degree of the material to be processed is:

[0044] ① Calculation of total sampling weight, according to (representative sampling method in mineral processing industry) G = Kd t , take K = 0.1, t = 2, if the maximum particle size in the material is d = 4mm, then the final sampling weight G = 1.6kg.

[0045] ② Calculation of sampling times. The volume of each sampling is ~2 cubic centimeters. The mass M of each sampling is calculated based on the bulk density. The number of samplings N is obtained by G / M. The samples are numbered from 1 to N.

[0046] ③ Determination: Determine the moisture content, median particle size, calorific value material content and permeability coefficient of each sample.

[0047] ④Compare and count, summarize the four major parameters of all samples and take the average value as the macro-overall parameter, which is also the benchmark parameter. Compare the four major parameters of each sample with the average value (the macro-overall parameter). The acceptable deviation of moisture content is ±10%, the acceptable deviation of median particle size is ±20%, the acceptable deviation of calorific value material content is ±30%, and the acceptable deviation of permeability coefficient is ±10%. After comparison, each time a sample parameter falls within the acceptable deviation range is recorded. After the statistics are completed, the statistical number of times the moisture content, median particle size, calorific value material content, and permeability coefficient of each sample are within the acceptable range will be obtained, which will be recorded as

[0048] ⑤ Weight and calculation: Different weights are assigned to the four parameters (water content, median particle size, calorific value material content, and permeability coefficient) according to their influence on the high temperature and anoxic reaction, which are 30%, 25%, 10%, and 35% respectively. The degree of homogenization is calculated by multiplying the weights of the four parameters by the sum of the proportion of the statistical times within the acceptable range.

[0049] Right now

[0050]

[0051] See also Figure 2 The pretreatment device diagram includes seven modules: S1 concentration module, S2 dehydration module, S3 dissociation module, S4 drying module, S5 batching module, S6 homogenization module, and S7 molding module.

[0052] The S1 thickening module comprises an S11 slurry mixing tank, an S12 mud pump and an S13 thickening tank which are connected in sequence, wherein the discharge port of the S11 slurry mixing tank is connected to the feed port of the S12 mud pump, and the discharge port of the S12 mud pump is connected to the S13 thickening tank through a pipeline;

[0053] The S2 dehydration module includes an S21 filter press mud pump and an S22 filter press, wherein the S21 filter press mud pump is connected to the S22 filter press through a pipeline, and an S23 material receiving wide belt is provided under the S22 filter press for transporting the filtered material to the S3 dissociation module;

[0054] The S3 dissociation module includes an S31 blockage clearing machine and an S33 cage crusher. The S31 blockage clearing machine is arranged below the S23 material receiving wide belt. An S32 crushing pulling belt scale is arranged between the discharge port of the S31 blockage clearing machine and the feed port of the S33 cage crusher, which is used to transport the block materials to the S33 cage crusher. The discharge port of the S33 cage crusher is provided with an S34 vibrating screen. The S34 vibrating screen is inclined, and an S36 under-screen belt is arranged below the screen. The S3 dissociation module also includes an S35 bucket elevator. The feed port of the S35 bucket elevator is connected to the downward inclined side of the S34 vibrating screen, and the discharge port of the S35 bucket elevator is connected to the S33 cage crusher. Qualified bulk materials are transported to the S4 drying module by the S36 under-screen belt, and unqualified bulk materials are returned to the S33 cage crusher by the S35 bucket elevator for further crushing.

[0055] The S4 drying module includes an S41 buffer bin and an S43 dryer. The S41 buffer bin is arranged below the S36 screen belt. An S42 drying pull-type belt scale is arranged between the S41 buffer bin discharge port and the S43 dryer feed port. Qualified bulk materials are measured by the S42 drying pull-type belt scale and then transported to the S43 dryer. The heat source used by the S43 dryer includes hot air or hot flue gas after pyrolysis flue gas heat exchange, and externally supplied steam.

[0056] The S5 batching module includes an S51 batching belt, an S52 first auxiliary material bin, an S53 second auxiliary material bin, and an S54 oil sludge bin; the S51 batching belt is located between the S43 dryer outlet and the S54 oil sludge bin feed port, and is used to transport the dried bulk material to the S54 oil sludge bin; the S52 first auxiliary material bin and the S53 second auxiliary material bin are used to add auxiliary fuel or catalyst; the S52 first auxiliary material bin is connected to a S55 first auxiliary material reduction scale, the S53 second auxiliary material bin is connected to a S56 second auxiliary material reduction scale, and the S54 oil sludge bin is provided with a S57 batching pull-type belt scale for quantitative batching; the number of auxiliary material bins in the S5 batching module is 2 or more, and each auxiliary material bin is connected to an auxiliary material reduction scale.

[0057] The S6 homogenizing module includes an S61 strong mixing belt arranged below the S55 first auxiliary material reduction scale, the S56 second auxiliary material reduction scale and the S57 batching pull-type belt scale, and an S62 strong mixer arranged under the S61 strong mixing belt;

[0058] The S7 molding module includes an S71 molding belt, an S72 molding buffer bin, and an S74 molding machine; the S71 molding belt is located between the discharge port of the S62 intensive mixer and the feed port of the S72 molding buffer bin, and is used to transport the mixed materials to the S72 molding buffer bin; the S72 molding buffer bin is provided with an S73 molding pull-type belt scale, which is used to quantitatively feed the materials to the S74 molding machine. Finally, the pretreated materials are output by the S74 molding machine, and then the pretreated materials are sent to the high-temperature anoxic reaction device. Compared with directly putting the sludge into the high-temperature anoxic reaction device, or simply drying and controlling the water before putting it into the high-temperature reaction device, the sludge requires less energy after pretreatment by the present invention, and a faster reaction speed and more valuable reaction by-products can be obtained.

[0059] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention rather than to limit it. Although the present invention is illustrated with reference to the above embodiments, ordinary technicians in the relevant field should understand that the specific implementation methods of the present invention can still be modified or replaced by equivalents, and any modifications or equivalent replacements that do not depart from the spirit and scope of the present invention should be included in the scope of the present claims.

Claims

1. A pretreatment method for improving high temperature and hypoxia reaction, characterized in that: The method is to pre-treat the material to be treated that needs to undergo a high-temperature anoxic reaction according to its physical and chemical properties to adjust the properties of the material to be treated, and specifically includes the following steps: Step 1, concentration: if the moisture content of the material to be treated is less than 60%, directly proceed to step 2; if the moisture content of the material to be treated is between 60% and 99.9%, reduce the moisture content of the material to be treated to less than 60% by gravity sedimentation, centrifugation, adsorption, electrochemical enrichment, flocculation, and mechanical classification dehydration; Step 2, dehydration: if the moisture content of the material to be treated is lower than 40%, directly proceed to step 3; if the moisture content of the material to be treated is between 40% and 60%, the moisture content of the material to be treated is reduced by positive pressure filtration, negative pressure filtration, centrifugation, mechanical graded dehydration, and chemical reaction dehydration until the moisture content is lower than 40%; Step 3, dissociation: if the particle size of the material to be processed is less than 30mm, directly proceed to step 4; if the particle size of the material to be processed is greater than 30mm, separate or disperse the liquid or solid with calorific value in the material to be processed from the original surrounding medium by crushing, grinding and analysis, so that the particle size of the material to be processed is less than 30mm; Step 4, drying: if the moisture content of the material to be processed is less than 20%, directly proceed to step 5; if the moisture content of the material to be processed is between 20% and 40%, the water and other volatile components in the material to be processed are taken away by low-temperature hot gas, and the moisture content of the material to be processed is reduced until the moisture content is less than 20%; Step 5, batching: If the reaction potential barrier of the material to be processed is low, that is, when the temperature is below 500°C, the thermal energy RT is greater than the activation energy E a , then directly go to step 6; if the reaction potential barrier of the material to be treated is high, the temperature below 500℃ does not satisfy the requirement that the thermal energy RT is greater than the activation energy E a , then add auxiliary fuel with lower reaction potential barrier or catalyst to reduce reaction potential barrier to the material to be treated until the overall reaction potential barrier is reduced, so that the temperature below 500℃ can satisfy the requirement that thermal energy RT is greater than activation energy E a ; Step 6, homogenization: if the homogenization degree of the material to be processed is above 60%, proceed to step 7; if the homogenization degree of the material to be processed is lower than 60%, the material to be processed is mixed by a mobile mechanical mixer or a fixed mixing device to form a mixed material with a homogenization degree of more than 60% and a uniform texture; Step 7, molding: If the porosity of the material to be processed is above 25%, it will directly enter the high-temperature anoxic reaction; if the porosity of the material to be processed is lower than 25%, the material to be processed will be molded by extrusion or rolling.

2. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: The material to be processed is a liquid or solid or a solid-liquid mixture with a calorific value greater than 1 MJ / Kg when the water content is less than 40%, and the material to be processed includes oil sludge.

3. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: The high temperature is between 300°C and 1300°C.

4. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: The low-temperature hot gas in step 4 is one of steam, waste flue gas, air, and inert gas, and its temperature is between 100°C and 500°C.

5. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: In step 5, the auxiliary fuel includes pulverized coal, sawdust, and rice husk, and the catalyst includes clay and lime; the amount of the auxiliary fuel or catalyst added is 0.1% to 40%.

6. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: The degree of homogenization in step 6 is determined by assigning weights of 30%, 25%, 10%, and 35% to the moisture content, median particle size, calorific value material content, and permeability coefficient of the material, respectively.

7. A pretreatment method for improving high temperature and hypoxia reaction according to claim 1, characterized in that: The shapes of the molding in step 7 include honeycomb, columnar, pillow, spherical or irregular granular shapes.

8. A pretreatment device based on the pretreatment method for improving high temperature anoxic reaction according to claim 1, characterized in that: It includes 7 modules: S1 concentration module, S2 dehydration module, S3 dissociation module, S4 drying module, S5 batching module, S6 homogenization module and S7 molding module; The S1 thickening module comprises an S11 slurry mixing tank, an S12 mud pump and an S13 thickening tank which are connected in sequence, wherein the discharge port of the S11 slurry mixing tank is connected to the feed port of the S12 mud pump, and the discharge port of the S12 mud pump is connected to the S13 thickening tank through a pipeline; The S2 dehydration module includes an S21 filter press mud pump and an S22 filter press, wherein the S21 filter press mud pump is connected to the S22 filter press through a pipeline, and an S23 material receiving wide belt is provided under the S22 filter press for transporting the filtered material to the S3 dissociation module; The S3 dissociation module includes an S31 blockage clearing machine and an S33 cage crusher. The S31 blockage clearing machine is arranged below the S23 material receiving wide belt. A S32 crushing pull-type belt scale is arranged between the discharge port of the S31 blockage clearing machine and the feed port of the S33 cage crusher, which is used to transport the block material to the S33 cage crusher. The discharge port of the S33 cage crusher is provided with an S34 vibrating screen, which is inclined, and an S36 under-screen belt is arranged below the screen. The S4 drying module includes an S41 buffer bin and an S43 dryer, wherein the S41 buffer bin is arranged below the S36 under-screen belt, and a S42 drying pull-type belt scale is arranged between the S41 buffer bin discharge port and the S43 dryer feed port; The S5 batching module includes an S51 batching belt, an S52 first auxiliary silo, an S53 second auxiliary silo, and an S54 oil sludge silo; the S51 batching belt is arranged between the S43 dryer discharge port and the S54 oil sludge silo feed port, and is used to transport the dried bulk material to the S54 oil sludge silo; the S52 first auxiliary silo and the S53 second auxiliary silo are used to add auxiliary fuel or catalyst, the S52 first auxiliary silo is connected to a S55 first auxiliary material reduction scale, the S53 second auxiliary silo is connected to a S56 second auxiliary material reduction scale, and the S54 oil sludge silo is provided with a S57 batching pull-type belt scale for quantitative batching; The S6 homogenizing module includes an S61 strong mixing belt arranged below the S55 first auxiliary material reduction scale, the S56 second auxiliary material reduction scale and the S57 batching pull-type belt scale, and an S62 strong mixer arranged under the S61 strong mixing belt; The S7 molding module includes an S71 molding belt, an S72 molding buffer bin, and an S74 molding machine; the S71 molding belt is located between the discharge port of the S62 intensive mixer and the feed port of the S72 molding buffer bin, and is used to transport the mixed materials to the S72 molding buffer bin; the S72 molding buffer bin is provided with an S73 molding pull-type belt scale, which is used to quantitatively feed the materials to the S74 molding machine; The S3 dissociation module also includes an S35 bucket elevator, the feed port of the S35 bucket elevator is connected to the downwardly inclined side of the S34 vibrating screen, the discharge port of the S35 bucket elevator is connected to the S33 cage crusher, and the qualified bulk materials are transported to the S4 drying module by the S36 under-screen belt, and the unqualified bulk materials are returned by the S35 bucket elevator to the S33 cage crusher for further crushing; The number of auxiliary material bins in the S5 batching module is 2 or more, and each of the auxiliary material bins is connected to an auxiliary material reduction scale.

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