A chemical chaining gasification method for iron-rich sludge

Abstract

The present application relates to a chemical chain gasification method for iron-rich sludge, comprising: sequentially performing filter pressing and crushing treatment on the iron-rich sludge to generate iron-rich sludge particles with a moisture content of 40% to 50%; introducing an iron-based oxygen carrier and the iron-rich sludge particles into a fluidized bed reactor for a chemical chain gasification reaction, so that the iron-rich sludge particles are ashed to generate a supplementary oxygen carrier during the gasification reaction; performing the chemical chain gasification reaction based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone the gasification reaction. Based on this method, the overall performance decay of the oxygen carrier can be delayed and the use cost of the oxygen carrier can be reduced; at the same time, the sludge can be more fully utilized to improve resource utilization.

Description

Technical Field

[0001] The present application relates to the technical field of industrial solid waste resource utilization, and in particular to a chemical chain gasification method for iron-rich sludge. Background Art

[0002] Chemical chaining technology is a carbon capture and utilization technology that aims to reduce carbon dioxide emissions and achieve carbon neutrality. This technology reduces dependence on fossil fuels and reduces greenhouse gas emissions by capturing and utilizing carbon dioxide in chemical reactions and converting it into useful chemicals or fuels. Chemical chaining technology generally includes two main steps: first, capturing carbon dioxide through chemical reactions, and then using this captured carbon dioxide for chemical conversion or synthesis.

[0003] In chemical chaining technology, various oxygen carriers or catalysts are usually used to promote the capture and conversion process of carbon dioxide. These oxygen carriers or catalysts can absorb and release oxygen in chemical reactions, thereby achieving the capture and utilization of carbon dioxide. The chemical chaining technology of sludge mainly converts organic matter in sludge into synthesis gas or other combustible gases through chemical chaining gasification technology, thereby achieving energy recovery and utilization. However, due to the effects of mechanical, thermal and chemical stresses, oxygen carriers have serious performance degradation phenomena such as wear and escape, phase separation, agglomeration and sintering, which limits the large-scale commercial application of chemical chaining technology. Summary of the invention

[0004] The chemical chaining gasification method for iron-rich sludge provided in an embodiment of the present invention at least solves the problem in the related art that the performance of oxygen carriers decays too quickly during the chemical chaining gasification process of sludge.

[0005] In a first aspect, an embodiment of the present invention provides a chemical chaining gasification method for iron-rich sludge, comprising:

[0006] The iron-rich sludge is subjected to filter pressing and crushing treatment in sequence to generate iron-rich sludge particles with a moisture content of 40% to 50%;

[0007] Passing the iron-based oxygen carrier and the iron-rich sludge particles into a fluidized bed reactor for a chemical chain gasification reaction, so that the iron-rich sludge particles are ashed to generate supplementary oxygen carriers during the gasification reaction;

[0008] The chemical chaining gasification reaction is carried out based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone the gasification reaction.

[0009] According to an embodiment of the present invention, the diameter of the iron-rich sludge particles is comprised between 0.5 mm and 1 mm.

[0010] According to an embodiment of the present invention, the iron-based oxygen carrier includes at least one of the following: a copper-iron spinel oxygen carrier, a perovskite-type oxygen carrier, and a sludge ash-formed oxygen carrier.

[0011] According to an embodiment of the present invention, the molecular formula of the copper iron spinel oxygen carrier is CuFe2O4, and the molecular formula of the perovskite oxygen carrier is CaMn 0.5 Fe 0.5 O 3-δ .

[0012] According to an embodiment of the present invention, the copper-iron spinel oxygen carrier is obtained based on the following method:

[0013] The red mud is subjected to a pulverizing treatment, a drying treatment and a sieving treatment in sequence to obtain a red mud powder, wherein the particle size of the red mud powder is less than 75 μm, the drying temperature of the drying treatment is 105 degrees Celsius, and the drying time is 4 hours;

[0014] Mixing the red mud powder, copper oxide and water to generate a first mixture, wherein the water content of the first mixture is 10% to 15%, and the mass ratio of the red mud powder to the copper oxide is 17:3;

[0015] The first mixture is subjected to sequential balling, shade drying and baking treatments to obtain the copper-iron spinel oxygen carrier.

[0016] According to an embodiment of the present invention, the first mixture is subjected to sequential balling, shade drying and drying to obtain the copper-iron spinel oxygen carrier, comprising:

[0017] The first mixture is subjected to a pelletizing process to generate a first mixture pellet, wherein the particle size of the first mixture pellet is 0.5 mm to 1 mm;

[0018] Placing the first mixture ball blank in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the first mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours;

[0019] Based on a first preset drying condition, placing the first mixture ball blank after the shade drying process in a drying device for drying process to obtain the copper-iron spinel oxygen carrier;

[0020] The first preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, and then heating it to 900 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0021] According to an embodiment of the present invention, the perovskite-type oxygen carrier is obtained based on the following method:

[0022] The red mud, manganese sand and calcium hydroxide are crushed, dried and sieved respectively to obtain red mud powder, manganese sand powder and calcium oxide powder, wherein the particle sizes of the red mud powder, the manganese sand powder and the calcium oxide powder are less than 75 μm, the drying temperature of the drying treatment is 105 degrees Celsius, and the drying time is 4 hours;

[0023] The red mud powder, the manganese sand powder, the calcium oxide powder and water are mixed to generate a second mixture, wherein the water content of the second mixture is 10% to 15%, and the mass ratio of the red mud powder, the manganese sand powder and the calcium oxide powder is 36:38:26;

[0024] The second mixture is subjected to sequential balling, shade drying and baking treatments to obtain the perovskite-type oxygen carrier.

[0025] According to an embodiment of the present invention, the second mixture is subjected to sequential balling, shade drying and drying to obtain the perovskite-type oxygen carrier, comprising:

[0026] The second mixture is subjected to a pelletizing process to generate a second mixture pellet, wherein the particle size of the second mixture pellet is 0.5 mm to 1 mm;

[0027] Placing the second mixture ball blank in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the second mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours;

[0028] Based on the second preset drying condition, placing the second mixture pellet after the shade drying process in a drying device for drying process to obtain the perovskite type oxygen carrier;

[0029] The second preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, and then heating it to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0030] According to an embodiment of the present invention, the sludge ash shaped oxygen carrier is obtained based on the following method:

[0031] The iron-rich sludge is crushed and dried in sequence to obtain sludge particles, wherein the drying temperature of the drying process is 105 degrees Celsius and the drying time is 4 hours;

[0032] The sludge particles are subjected to ash treatment and sieving treatment in sequence to obtain sludge ash powder, wherein the particle size of the sludge ash powder is less than 75 μm;

[0033] mixing the sludge ash powder and water to obtain a third mixture;

[0034] The third mixture is subjected to sequential pelletizing, shade drying and oven drying processes to obtain the sludge ash shaped oxygen carrier.

[0035] According to an embodiment of the present invention, the third mixture is subjected to sequential pelletizing, shade drying and drying to obtain the sludge ash shaped oxygen carrier, comprising:

[0036] The third mixture is subjected to a pelletizing process to generate a third mixture pellet, wherein the pellet has a particle size of 0.5 mm to 1 mm;

[0037] The third mixture ball blank is placed in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the third mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours;

[0038] Based on the third preset drying condition, placing the third mixture pellet after the shade drying process in a drying device for drying process to obtain the sludge ash shaped oxygen carrier;

[0039] The second preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, and then heating it to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0040] Beneficial effects of the embodiments of the present invention: The chemical chain gasification method for iron-rich sludge provided by the embodiments of the present invention can delay the overall performance decay of the oxygen carrier and reduce the use cost of the oxygen carrier. Specifically, by sequentially filtering and crushing the iron-rich sludge, iron-rich sludge particles with a water content of 40% to 50% are generated, and then the iron-based oxygen carrier and the above-mentioned iron-rich sludge particles are introduced into a fluidized bed reactor for chemical chain gasification reaction, so that the iron-rich sludge particles are ashed during the gasification reaction to generate supplementary oxygen carriers, so that the chemical chain gasification reaction can be continued based on the above-mentioned supplementary oxygen carriers, iron-based oxygen carriers and iron-rich sludge particles that have not undergone gasification reaction. Based on the above method, the catalytic and oxygen-carrying effects of iron oxides in sludge ash can be utilized to delay the overall performance decay of the oxygen carrier, reduce the use cost of the oxygen carrier, and promote the large-scale application of chemical chain technology; at the same time, the supplementary oxygen carrier is formed by self-growth and self-renewal of iron-rich sludge particles during the reaction process, the process is simple, and the use cost is low; finally, the sludge can be more fully utilized to improve resource utilization.

[0041] The details of one or more embodiments of the invention are set forth in the following drawings and description so that other features, objects, and advantages of the invention are more readily apparent. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the prior art descriptions. Obviously, the drawings described below are only some embodiments of the present invention, and for ordinary technicians in this field, other embodiments can be obtained based on these drawings without creative work.

[0043] Figure 1 A flow chart of a chemical chaining gasification method for iron-rich sludge provided as an exemplary embodiment of the present invention.

[0044] Figure 2 A flow chart of a method for preparing a copper-iron spinel oxygen carrier is provided as an exemplary embodiment of the present invention.

[0045] Figure 3 A flow chart of a method for preparing a perovskite-type oxygen carrier provided by an exemplary embodiment of the present invention.

[0046] Figure 4 A flow chart of a method for preparing a sludge ash molded oxygen carrier is provided as an exemplary embodiment of the present invention.

[0047] Figure 5 A schematic diagram of XRD test results of an iron-based oxygen carrier provided by an exemplary embodiment of the present invention.

[0048] Figure 6 A diagram showing changes in the composition of the chemical looping gasification multi-cycle synthesis gas corresponding to a copper-iron spinel oxygen carrier provided as an exemplary embodiment of the present invention.

[0049] Figure 7 A diagram showing changes in the composition of the chemical chaining gasification multi-cycle synthesis gas corresponding to a perovskite-type oxygen carrier provided by an exemplary embodiment of the present invention.

[0050] Figure 8 A diagram showing changes in the components of a chemical chaining gasification multi-cycle synthesis gas corresponding to a sludge ash formed oxygen carrier provided as an exemplary embodiment of the present invention.

[0051] Fig. 9 It is the SEM-EDS picture of the oxygen carrier after the cycles of Examples 1-5 provided by the present invention. DETAILED DESCRIPTION

[0052] Embodiments of the present embodiment will be described in more detail below with reference to the accompanying drawings. Although certain embodiments of the present embodiment are shown in the accompanying drawings, it should be understood that the present embodiment can be implemented in various forms and should not be construed as being limited to the embodiments set forth herein, which are instead provided for a more thorough and complete understanding of the present embodiment. It should be understood that the drawings and embodiments of the present embodiment are only for exemplary purposes and are not intended to limit the scope of protection of the present embodiment.

[0053] Sludge is the main solid waste generated in the sewage treatment process. It has a very high water content and is mainly composed of organic matter. It also contains nitrogen (N), phosphorus (P), toxic pollutants, inorganic compounds, pathogens and other microbial pollutants. With the growth of population and economic activities, the output of sludge has increased rapidly. At present, the main treatment methods for sludge are thermochemical conversion methods such as incineration and gasification. While obtaining value-added energy (heat energy, combustible gas, bio-oil, biochar, etc.), it also produces a large amount of ash, which is mainly composed of silicon (Si), calcium (Ca), P (phosphorus), aluminum (Al) and iron (Fe).

[0054] In the chemical chain gasification process of sludge, the organic matter in the sludge is converted into synthesis gas or other combustible gases, thereby realizing energy recovery and utilization. However, due to the effects of mechanical, thermal and chemical stresses, the oxygen carrier suffers from serious performance degradation such as wear and escape, phase separation, agglomeration and sintering, which limits the large-scale commercial application of chemical chain technology.

[0055] In order to solve the problem in the related art that the performance of oxygen carriers decays too quickly during the chemical chaining gasification process of sludge, an embodiment of the present invention provides a chemical chaining gasification method for iron-rich sludge.

[0056] The technical solutions provided by various embodiments of the present invention are described in detail below in conjunction with the accompanying drawings.

[0057] Figure 1 A flow chart of a chemical chaining gasification method for iron-rich sludge provided by an exemplary embodiment of the present invention. Figure 1 , the method comprises the following steps.

[0058] S101, the iron-rich sludge is subjected to filter pressing and crushing treatment in sequence to generate iron-rich sludge particles with a moisture content of 40% to 50%.

[0059] S102, introducing the iron-based oxygen carrier and the iron-rich sludge particles into a fluidized bed reactor for a chemical chain gasification reaction, so that the iron-rich sludge particles are ashed to generate supplementary oxygen carriers during the gasification reaction.

[0060] S103, a chemical chain gasification reaction is carried out based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone the gasification reaction.

[0061] In this embodiment, when the iron-rich sludge is subjected to filter pressing and crushing treatment in sequence, the sludge moisture can first be reduced to 40% to 50% by mechanical filter pressing. Subsequently, the sludge after filter pressing can be crushed and sieved mechanically so that the particle size of the crushed iron-rich sludge is 0.5 mm to 1 mm, and the above-mentioned iron-rich sludge particles can be obtained.

[0062] After the iron-rich sludge particles are obtained, they can be subjected to a chemical chain gasification reaction. Specifically, the iron-based oxygen carrier and the iron-rich sludge particles can be introduced into a fluidized bed reactor for a chemical chain gasification reaction, so that the iron-rich sludge particles can be ashed to generate supplementary oxygen carriers during the gasification reaction.

[0063] Specifically, the ashification process of the sludge in the above embodiment is the process in which the sludge added at the beginning of the cycle in the chemical chain gasification process undergoes pyrolysis, gasification, and residual carbon combustion to form ash. After the sludge ash undergoes gasification reaction, the shrink core collapses to form ash particles and deposits on the solid surface, completing the self-growth process of the sludge ash particles.

[0064] In this embodiment, the fluidized bed reactor can switch between the gasification reactor and the air reactor by switching the air inlet atmosphere, and a cyclone separator is provided at the reactor outlet, which can screen and separate the materials. Specifically, the iron-based oxygen carrier can be replaced by the cyclone separator, and part of the oxygen carrier can be separated by the cyclone separator to adjust the ratio of sludge to oxygen carrier during the gasification process, thereby obtaining the best quality syngas.

[0065] After the supplementary oxygen carrier is generated, a chemical chain gasification reaction can be carried out based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone gasification reaction.

[0066] In this embodiment, the iron-based oxygen carrier includes at least one of the following: a copper-iron spinel oxygen carrier, a perovskite-type oxygen carrier, and a sludge ash-formed oxygen carrier.

[0067] Among them, the molecular formula of copper iron spinel oxygen carrier is CuFe2O4, and the molecular formula of perovskite oxygen carrier is CaMn 0.5 Fe 0.5 O 3-δ .

[0068] In an optional embodiment, after a chemical chain gasification reaction is carried out based on supplementary oxygen carriers, iron-based oxygen carriers and iron-rich sludge particles that have not undergone gasification reaction, the air inlet atmosphere of the fluidized bed reactor is switched to air, the sludge ash is crushed, floated and discharged, and the iron-based oxygen carrier and sludge ash supplementary oxygen carrier particles are regenerated, thereby completing a chemical chain gasification cycle of iron-rich sludge. Figure 2A flow chart of a method for preparing a copper-iron spinel oxygen carrier provided by an exemplary embodiment of the present invention. Figure 2 The preparation method of the copper-iron spinel oxygen carrier (CuFe2O4) includes the following steps.

[0069] S201, pulverizing, drying and screening the red mud in sequence to obtain red mud powder, wherein the particle size of the red mud powder is less than 75 μm, the drying temperature of the drying treatment is 105 degrees Celsius, and the drying time is 4 hours;

[0070] S202, mixing red mud powder, copper oxide and water to generate a first mixture, wherein the water content of the first mixture is 10% to 15%, and the mass ratio of the red mud powder to the copper oxide is 17:3;

[0071] S203, sequentially subjecting the first mixture to pelletization, air drying and baking treatments to obtain a copper-iron spinel oxygen carrier.

[0072] In this embodiment, after the red mud is crushed and dried in sequence, the treated red mud needs to be screened to obtain red mud powder. In practical applications, the mesh number of the sieve for screening the red mud can be 200 mesh. Based on the 200 mesh sieve, red mud powder with a particle size of less than 75 μm can be obtained. Subsequently, the red mud powder is dried at a drying temperature of 105 degrees Celsius for 4 hours until the red mud powder is dried to a constant weight.

[0073] Subsequently, the red mud powder, copper oxide and water are mixed. Specifically, the red mud powder and copper oxide can be mixed mechanically, that is, stirred for 3 to 6 hours by a cantilever electric stirrer, so that the red mud powder and copper oxide are fully mixed. During the stirring process, water can be sprayed while stirring until the water content of the mixture is between 10% and 15%.

[0074] After the first mixture is obtained, it can be subjected to balling, shade drying and oven drying processes in sequence.

[0075] In an optional embodiment, first, the first mixture can be pelletized to generate a first mixture pellet, wherein the particle size of the first mixture pellet is 0.5 mm to 1 mm. Specifically, the first mixture can be pelletized by an industrial-scale extrusion spheronization method.

[0076] In the present embodiment, the extrusion spheronization method is a common granulation process, which is usually used to prepare a granular solid product. Its basic principle is to extrude the raw material into a spherical shape through an extruder, and then the extruded material is shaped into a spherical shape through a spheronization machine. In the extrusion spheronization method, the first mixture is first extruded into a spherical shape through an extruder, usually by extruding the material through the screw of the extruder and discharging the material from the molding port to form a continuous strip material. Then, these strip materials are transported to the spheronization machine, and the spheronization machine gradually spheronizes the strip materials through the rotary motion of the drum, and finally forms a granular finished product.

[0077] Subsequently, the first mixture ball blank is placed in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the first mixture ball blank after shade drying, and the shade drying time includes 24 hours to 48 hours.

[0078] Finally, based on the first preset drying condition, the first mixture pellet after the shade drying is placed in a drying device for drying to obtain the copper-iron spinel oxygen carrier.

[0079] Among them, the first preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, then heating it to 900 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0080] In this embodiment, the drying device may include a muffle furnace or the like.

[0081] Figure 3 A flowchart of a method for preparing a perovskite-type oxygen carrier is provided as an exemplary embodiment of the present invention. Figure 3 The perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) comprises the following steps.

[0082] S301, respectively crushing, drying and screening the red mud, manganese sand and calcium hydroxide to obtain red mud powder, manganese sand powder and calcium oxide powder. The particle sizes of the red mud powder, manganese sand powder and calcium oxide powder are less than 75 μm. The drying temperature of the drying treatment is 105 degrees Celsius and the drying time is 4 hours.

[0083] S302, mixing red mud powder, manganese sand powder, calcium oxide powder and water to generate a second mixture, the water content of the second mixture is 10% to 15%, and the mass ratio of red mud powder, manganese sand powder and calcium oxide powder is 36:38:26.

[0084] S303, the second mixture is subjected to sequential balling, shade drying and baking treatments to obtain a perovskite-type oxygen carrier.

[0085] In this embodiment, after the red mud, manganese sand and calcium hydroxide are crushed and dried, they need to be screened to obtain red mud powder, manganese sand powder and calcium oxide powder. In practical applications, the mesh number of the sieve for screening red mud, manganese sand and calcium hydroxide can be 200 mesh. Based on the 200 mesh sieve, red mud powder, manganese sand powder and calcium oxide powder with a particle size of less than 75 μm can be obtained. Subsequently, the red mud powder, manganese sand powder and calcium oxide powder are dried at a drying temperature of 105 degrees Celsius for 4 hours until the red mud powder, manganese sand powder and calcium oxide powder are dried to constant weight.

[0086] Subsequently, the red mud powder, manganese sand powder and calcium oxide powder are mixed with water. Specifically, the red mud powder, manganese sand powder and calcium oxide powder can be mixed mechanically, that is, by a cantilever electric stirrer, for 3 to 6 hours to fully mix the red mud powder, manganese sand powder and calcium oxide powder. During the stirring process, water can be sprayed while stirring until the water content of the mixture is between 10% and 15%.

[0087] After the second mixture is obtained, it can be subjected to balling, shade drying and oven drying processes in sequence.

[0088] In an optional embodiment, first, the second mixture can be pelletized to generate second mixture pellets, wherein the particle size of the second mixture pellets is 0.5 mm to 1 mm. Specifically, the second mixture can be pelletized by an industrial-scale disc pelletization method.

[0089] In this embodiment, the disc granulation method is a common granulation process, which is used to make powdered or granular raw materials into granular solid products, and is usually used in the fields of pharmaceuticals, chemicals, food, etc. The basic principle of this process is to roll, stack and granulate the raw materials through a rotating disc, and finally form a granular finished product.

[0090] In the disc granulation method, the second mixture is first evenly sprayed on the rotating disc, and then the disc starts to rotate. During the rotation process, the raw material is subjected to the centrifugal force and friction force, and gradually forms granular solid particles. At the same time, by adding an appropriate amount of binder or lubricant, it can help the particle forming and improve the strength of the particles.

[0091] Subsequently, the second mixture ball blank is placed in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the shade-dried second mixture ball blank, and the shade drying time includes 24 hours to 48 hours.

[0092] Finally, based on the second preset drying condition, the second mixture pellet after the air drying process is placed in a drying device for drying process to obtain a perovskite type oxygen carrier;

[0093] Among them, the second preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, and then heating it to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0094] In this embodiment, the drying device may include a muffle furnace or the like.

[0095] Figure 4 A flow chart of a method for preparing a sludge ash shaped oxygen carrier according to an exemplary embodiment of the present invention. Figure 4 The preparation method of the sludge ash molded oxygen carrier includes the following steps.

[0096] S401, the iron-rich sludge is crushed and dried in sequence to obtain sludge particles. The drying temperature of the drying treatment is 105 degrees Celsius and the drying time is 4 hours.

[0097] S402, ash the sludge particles and screen them in turn to obtain sludge ash powder, wherein the particle size of the sludge ash powder is less than 75 μm.

[0098] S403, mixing the sludge ash powder and water to obtain a third mixture.

[0099] S404, sequentially subjecting the third mixture to pelletizing, air-drying and oven drying to obtain a sludge ash shaped oxygen carrier.

[0100] In this embodiment, after the iron-rich sludge is subjected to sequential crushing and drying treatments to obtain sludge particles, the sludge particles can be subjected to sequential ashing and sieving treatments to obtain sludge ash powder.

[0101] In practical applications, when the sludge particles are ashed sequentially, the sludge particles can be evenly spread in a crucible, put into a muffle furnace at room temperature, and the temperature is raised to 500°C within 30 minutes under the conditions of natural ventilation and a 15mm gap at the furnace door, and then kept warm for 30 minutes, and then the temperature is raised to 815°C and roasted for 2.5 hours to complete the ashing of the sludge particles. In addition, the mesh number of the sieve for sieving the sludge particles can be 200 meshes.

[0102] In an optional embodiment, the third mixture is subjected to sequential pelletizing, shade drying and drying to obtain the sludge ash shaped oxygen carrier, which may specifically include:

[0103] First, the third mixture is pelletized to generate a third mixture pellet, wherein the particle size of the third mixture pellet is 0.5 mm to 1 mm. In this embodiment, the third mixture can be pelletized by a disc pelletization method.

[0104] Subsequently, the third mixture ball blank is placed in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the shade-dried third mixture ball blank, and the shade drying time includes 24 hours to 48 hours.

[0105] Finally, based on the third preset drying condition, the third mixture pellets after the shade drying are placed in a drying device for drying to obtain the sludge ash molded oxygen carrier.

[0106] Among them, the second preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping it warm for 2 hours, and then heating it to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping it warm for 6 hours.

[0107] In this embodiment, the drying device may include a muffle furnace or the like.

[0108] The chemical chaining gasification method of iron-rich sludge provided by the embodiment of the present invention is described below in conjunction with specific embodiments.

[0109] It should be noted that the sludge used in the following examples was taken from the same location. After testing and analysis, the sludge fuel analysis results are shown in Table 1:

[0110] Table 1 Sludge fuel analysis

[0111]

[0112] Among them, *O content is calculated by subtraction method.

[0113] The iron-rich sludge ash used in the following examples was tested by X-ray fluorescence spectroscopy (XRF), and the main chemical components and contents are shown in Table 2:

[0114] Table 2 Main chemical components of iron-rich sludge ash

[0115] chemical composition <![CDATA[SiO2]]> <![CDATA[Fe2O3]]> <![CDATA[P2O5]]> CaO <![CDATA[SO3]]> <![CDATA[Al2O3]]> MgO <![CDATA[K2O]]> <![CDATA[TiO2]]> MnO ZnO Content (wt / %) 29.516 20.096 16.726 12.664 7.246 6.379 4.000 1.698 1.001 0.262 0.249

[0116] The red mud used in the following examples was collected from the same location. After XRF testing, the main chemical components and their contents are shown in Table 3:

[0117] Table 3 Main chemical components of red mud

[0118] chemical composition <![CDATA[Na2O]]> MgO <![CDATA[Al2O3]]> <![CDATA[SiO2]]> CaO <![CDATA[TiO2]]> <![CDATA[Fe2O3]]> <![CDATA[K2O]]> Content (wt / %) 6.1407 0.1642 18.7015 20.1579 2.8823 4.0777 41.9228 0.1094

[0119] Example 1

[0120] This example is used to determine the performance attenuation of the copper-iron spinel oxygen carrier without the presence of sludge ash, and specifically includes:

[0121] First, a copper iron spinel oxygen carrier (CuFe2O4) is obtained by the copper iron spinel oxygen carrier preparation method in the above embodiment. In this embodiment, 425 grams of red mud powder and 75 grams of copper oxide powder are used; in addition, in the process of mixing the red mud powder, copper oxide and water, 55 grams of water are used.

[0122] Then, 30 grams of copper iron spinel oxygen carrier (CuFe2O4) was placed in a thermogravimetric analyzer for 30 times of reduction-oxidation regeneration. The specific temperature and gas control procedures were as follows:

[0123] (1) Heating process: In a 50 ml / min N2 atmosphere, heat to 800°C at a heating rate of 25°C / min.

[0124] (2) Reduction process: At 800°C, switch the carrier gas to 100 ml / min 5% H2 / 95% N2 and maintain it for 30 min to allow the oxygen carrier to be fully reduced.

[0125] (3) Gas washing process: After the reduction is completed, the carrier gas is switched to 50 ml / min N2 to exhaust the reducing gas in the device.

[0126] (4) Oxidation process: Switch the carrier gas to 100 ml / min air and maintain it for 15 min to complete the regeneration of the oxygen carrier.

[0127] In this embodiment, except for the first cycle which requires a heating process, the above parameter settings are repeated in the remaining cycles to complete 30 reduction-oxidation regenerations of the oxygen carrier to determine the performance attenuation of the copper-iron spinel oxygen carrier (CuFe2O4) in the absence of sludge ash.

[0128] Example 2

[0129] This embodiment is used to determine the performance attenuation of the copper-iron spinel oxygen carrier in the presence of sludge ash, specifically including:

[0130] First, copper iron spinel oxygen carrier (CuFe2O4) was prepared based on the same method as Example 1.

[0131] Then, 10 grams of copper iron spinel oxygen carrier (CuFe2O4) was taken and 30 chemical chain gasification experiments of iron-rich wet sludge were carried out using a small fluidized bed experimental device. The specific steps are as follows:

[0132] The iron-rich sludge particles prepared in the above embodiment are placed in a silo, and the feeding speed of the screw feeder is calibrated to achieve a continuous feeding amount within 3 minutes that satisfies O / C=1:2.75.

[0133] The copper-iron spinel oxygen carrier was added into the fluidized bed reactor through the feed port, with nitrogen as the carrier gas and the flow rate set to 6 L / min. The air tightness and fluidization state of the device were checked by the change in the outlet pressure. The fluidized bed reactor was heated to 800°C at a heating rate of 10°C / min, and then kept warm for 30 minutes to activate the oxygen carrier.

[0134] The spiral feeding device was turned on to start the sludge chemical chain gasification experiment. When the iron-rich sludge particles entered the reactor, a gas bag was connected at the outlet to collect the gas phase products for gas chromatography testing. When the feeding was stopped, the collection was stopped at the same time.

[0135] The carrier gas was switched to air at 6 L / min and maintained for 10 min to achieve the regeneration of the oxygen carrier and the combustion of the residual carbon produced in the gasification process, while also improving the lattice perfection of the ash.

[0136] The operations of sludge feeding and continuous switching of carrier gas were repeated to complete 30 cycles of sludge chemical chain gasification and iron-based oxygen carrier co-flow in iron-rich sludge ash.

[0137] After completing all the cycles and waiting for the reactor to cool to room temperature, the oxygen carrier was taken out for characterization testing to observe the performance degradation of the copper iron spinel oxygen carrier (CuFe2O4) in the presence of sludge ash (sludge was continuously added during the circulation process).

[0138] Example 3

[0139] This example is used to determine the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) performance degradation, including:

[0140] First, the perovskite-type oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ). In this embodiment, the red mud powder used is 180 grams, the red mud powder and manganese sand powder are 190 grams, and the calcium oxide powder is 130 grams; in addition, in the process of mixing the red mud powder, manganese sand powder, calcium oxide powder and water, the water used is 55 grams.

[0141] Then, take 30 grams of perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) was placed in a thermogravimetric analyzer for 30 times of reduction-oxidation regeneration, and the specific temperature and gas control procedures were as follows:

[0142] Heating process: heating to 800°C at a heating rate of 25°C / min in a 50ml / min N2 atmosphere;

[0143] Reduction process: at 800°C, switch the carrier gas to 100 ml / min 5% H2 / 95% N2 and keep it for 30 minutes to fully reduce the oxygen carrier;

[0144] Gas washing process: After the reduction is completed, the carrier gas is switched to 50ml / min N2 to exhaust the reducing gas in the device;

[0145] Oxidation process: switch the carrier gas to 100 ml / min air and maintain it for 15 min to complete the regeneration of the oxygen carrier.

[0146] In this embodiment, except for the first cycle which requires a heating process, the remaining cycles repeat the above parameter settings to complete 30 reduction-oxidation regenerations of the oxygen carrier to determine the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) performance degradation.

[0147] Example 4

[0148] This example is used to determine the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) performance degradation, including:

[0149] First, the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ).

[0150] Then, take 10 grams of perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ), a chemical chaining gasification experiment of iron-rich wet sludge was carried out using a small fluidized bed experimental device, and the specific steps are as follows:

[0151] The prepared iron-rich sludge particles are placed in the silo, and the feeding speed of the screw feeder is calibrated to achieve continuous feeding within 3 minutes to meet O / C = 1:2.75.

[0152] The oxygen carrier was added into the fluidized bed reactor through the feed port, with nitrogen as the carrier gas and the flow rate set to 6 L / min. The air tightness and fluidization state of the device were checked by the change in the outlet pressure. The fluidized bed reactor was heated to 800°C at a heating rate of 10°C / min, and then kept warm for 30 minutes to activate the oxygen carrier.

[0153] The spiral feeding device was turned on to start the sludge chemical chain gasification experiment. When the iron-rich sludge particles entered the reactor, a gas bag was connected at the outlet to collect the gas phase products for gas chromatography testing. When the feeding was stopped, the collection was stopped at the same time.

[0154] The carrier gas was switched to air at 6 L / min and maintained for 10 min to achieve the regeneration of the oxygen carrier and the combustion of the residual carbon produced in the gasification process, while also improving the lattice perfection of the ash.

[0155] The operations of sludge feeding and continuous switching of carrier gas were repeated to complete 30 chemical chain gasification processes of the sludge.

[0156] After all the cycles are completed, the reactor is cooled to room temperature, and the oxygen carrier is taken out for characterization test to determine whether the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) performance degradation.

[0157] Example 5

[0158] This embodiment provides a chemical chaining gasification method for iron-rich sludge, which specifically includes:

[0159] First, the sludge ash shaped oxygen carrier is obtained by the preparation method of the sludge ash shaped oxygen carrier in the above embodiment. Specifically, the iron-rich sludge is subjected to filter pressing to reduce its water content to 30% to 50%, the iron-rich sludge after filter pressing is crushed, and further dried at 105° C. for 4 hours to obtain dry iron-rich sludge particles.

[0160] Using a muffle furnace, the dried iron-rich sludge particles are evenly spread in a crucible and sent into a muffle furnace at room temperature. Under the conditions of natural ventilation and a 15mm gap at the furnace door, the temperature is raised to 500°C within 30 minutes, then kept warm for 30 minutes, and then the temperature is raised to 815°C and roasted for 2.5 hours to obtain sludge ash. After naturally cooling to room temperature, the sludge ash is mechanically crushed by a jaw crusher and sieved to obtain sludge ash powder with a particle size of less than 75μm.

[0161] 500 g of the sludge ash powder was mechanically stirred using a cantilever stirrer, and 55 g of water was sprayed while stirring to obtain a third mixture with a moisture content of about 10%.

[0162] The third mixture is placed in an industrial-scale disc granulator for molding to obtain spherical embryos with a particle size of 0.1-1 mm.

[0163] The spherical embryos were placed in a shaded place at 25°C for 24 hours to obtain dry spherical embryos. Then, a two-stage heating program was set up in a muffle furnace, firstly heating from the initial temperature to 350°C at a heating rate of 5°C / min and keeping it warm for 2 hours, and then heating from 350°C to 850°C at a heating rate of 5°C / min and keeping it warm for 6 hours to obtain the sludge ash shaped oxygen carrier.

[0164] Then, 10g of sludge ash was used to form oxygen carriers, and 30 chemical chain gasification experiments of iron-rich wet sludge were carried out using a small fluidized bed experimental device. The specific steps are as follows:

[0165] The prepared iron-rich sludge particles are placed in the silo, and the feeding speed of the screw feeder is calibrated to achieve continuous feeding within 3 minutes to meet O / C = 1:2.75.

[0166] The sludge ash molded oxygen carrier is added into the fluidized bed reactor through the feed port, nitrogen is used as the carrier gas, and the flow rate is set to 6L / min. The air tightness and fluidization state of the device are checked by the change of the outlet pressure. The fluidized bed reactor is set to heat to 800℃ at a heating rate of 10℃ / min, and then kept warm for 30 minutes to activate the sludge ash molded oxygen carrier.

[0167] The spiral feeding device was turned on to start the sludge chemical chain gasification experiment. When the iron-rich sludge entered the fluidized bed reactor, a gas bag was connected at the outlet to collect the gas phase product for gas chromatography testing. When the feeding was stopped, the collection was stopped at the same time.

[0168] The carrier gas was switched to air at 6 L / min and maintained for 10 min to achieve the regeneration of the sludge ash forming oxygen carrier and the combustion of the residual carbon produced in the gasification process, while also improving the lattice perfection of the ash.

[0169] Repeat the operation of sludge feeding and continuously switching the carrier gas to complete 30 reduction-oxidation cycles of the oxygen carrier in the sludge chemical chain gasification process.

[0170] Phase detection:

[0171] In order to analyze the above examples, the copper iron spinel oxygen carrier (CuFe2O4), the calcium perovskite type oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) and sludge ash-formed oxygen carriers were subjected to XRD tests to compare the chemical compositions of the three oxygen carriers. 0.5 Fe 0.5 O 3-δ ) and the XRD test results of the sludge ash molded oxygen carrier are as follows Figure 5 shown.

[0172] like Figure 5 As shown in Table 3, the red mud before calcination mainly contains Fe2O3, SiO2, Al2O3 and other substances, while the main components of the copper iron spinel oxygen carrier (CuFe2O4) formed after calcination are Cu .86 Fe 2.14 O4, perovskite-type oxygen carrier (CaMn 0.5 Fe 0.5 O 3-δ ) except CaMn 0.5 Fe 0.5 O 3-δ In addition, there is also some Fe2O3 that does not participate in the formation of perovskite; the main component of the sludge ash formed oxygen carrier is Fe2O3, the reason is that a large amount of SiO2 in the sludge ash can generate aluminum silicates with substances such as Al2O3 and Al(OH)3, avoiding the generation of substances such as ferric aluminate by Fe2O3 and Al2O3 and Al(OH)3, and maintaining the reactivity of the oxygen carrier, which shows that the three iron-based oxygen carriers were calcined successfully. In the present invention, the self-growth and self-renewal of iron-rich sludge ash particles into auxiliary oxygen carriers occurs under the conditions of the above three iron-based oxygen carriers.

[0173] Gas phase product testing:

[0174] The three oxygen carriers in Example 1, Example 3, and Example 5 were respectively obtained to conduct 30 reduction-oxidation cycle experiments of oxygen carriers in the sludge chemical chaining gasification process in a small fluidized bed, and the gas phase products were collected and analyzed by gas chromatography for the generation of synthesis gas components. Among them, the chemical chaining gasification multi-cycle synthesis gas component change diagrams corresponding to Example 1, Example 3, and Example 5 are shown as follows: Figure 6 , Figure 7 and Figure 8 shown.

[0175] The changes in the components of the syngas during the cycle can reflect the self-growth and self-renewal of the sludge ash particles into oxygen carriers. Figure 6 , Figure 7 and Figure 8 As the number of oxygen carrier cycles increases, the content of combustible gases such as hydrogen in the synthesis gas shows an overall downward trend, while the carbon dioxide content continues to rise. This shows that during the cycle, the continuously accumulated sludge ash self-grows and self-renews into an oxygen carrier, releasing lattice oxygen during the gasification process, causing the quality of the synthesis gas to decline, but correspondingly promoting the gasification degree of the sludge, and the carbon conversion rate has an increase of 2.57% to 6.21%.

[0176] like Figure 7 As shown, in the perovskite oxygen carrier (CaMn 0.5 Fe 0.5 O3-δ ) as the oxygen carrier, the changes in the composition of the synthesis gas are relatively stable, and the hydrogen content can still reach 39.62% after 20 cycles, which is mainly the result of the stability of the perovskite structure; Figure 8 As shown, when the gasification experiment was carried out using sludge ash particle oxygen carrier, the continuously accumulated sludge ash oxygen carrier caused large fluctuations in the components of the synthesis gas.

[0177] Physical product testing:

[0178] In this embodiment, the oxygen carrier after the oxidation regeneration cycle in the thermogravimetric analyzer and the sludge chemical chain gasification cycle in the fluidized bed reactor was characterized by a scanning electron microscope-energy dispersive X-ray spectrometer (SEM-EDS) to test the microscopic mechanism of the performance change of the iron-based oxygen carrier when the sludge ash is flowing. The SEM-EDS characterization test results are shown in FIG. Fig. 9 shown.

[0179] like Fig. 9 As shown, (1) to (5) are the SEM-EDS characterization test results of Examples 1 to 5, respectively. Under the switching atmosphere conditions in the thermogravimetric analyzer, the continuous release and acquisition of oxygen causes the oxygen carrier to have an obvious phase separation phenomenon as marked by the box in the figure, and the surface Fe phase is enriched, resulting in element islands. The position where the Fe phase migrates out exposes the support skeleton of the oxygen carrier, which will cause the performance of the oxygen carrier to be significantly attenuated. In the fluidized bed reactor, since sludge is added in each cycle, it is equivalent to the supplement of sludge ash oxygen carrier. In the fluidized state, sludge ash is in constant contact with the oxygen carrier. Under the surface competitive reaction, the lattice oxygen on the surface of the oxygen carrier is in situ suppressed by the iron phase of the sludge ash particles, and the iron phase enrichment and phase separation phenomenon are delayed. The oxygen carrying and catalytic effects assisted by sludge ash delay the trend of oxygen carrier performance attenuation.

[0180] An embodiment of the present invention further provides an electronic device, comprising: at least one processor; and a memory in communication with the at least one processor. The memory stores a computer program executable by the at least one processor, and when the computer program is executed by the at least one processor, the electronic device executes the method of the embodiment of the present invention.

[0181] It should be noted that the term "including" and its variations used in the embodiments of the present invention are open inclusions, that is, "including but not limited to". The term "based on" means "based at least in part on". The term "one embodiment" means "at least one embodiment"; the term "another embodiment" means "at least one other embodiment"; the term "some embodiments" means "at least some embodiments". The modifications of "one" and "multiple" mentioned in the embodiments of the present invention are illustrative rather than restrictive. Those skilled in the art should understand that unless the context clearly indicates otherwise, it should be understood as "one or more".

[0182] The user information (including but not limited to user device information, user personal information, etc.) and data (including but not limited to data used for analysis, stored data, displayed data, etc.) involved in the embodiments of the present invention are all information and data authorized by the user or fully authorized by all parties, and the collection, use and processing of relevant data must comply with relevant laws, regulations and standards of relevant countries and regions, and provide corresponding operation entrances for users to choose to authorize or refuse.

[0183] The various steps described in the method implementation methods provided in the embodiments of the present invention may be performed in different orders and / or in parallel. In addition, the method implementation methods may include additional steps and / or omit the steps shown. The scope of protection of the present invention is not limited in this respect.

[0184] The term "embodiment" in this specification refers to specific features, structures or characteristics described in conjunction with the embodiment that can be included in at least one embodiment of the present invention. The appearance of this phrase in various places in the specification does not necessarily mean the same embodiment, nor does it mean that it is mutually exclusive with other embodiments and is independent or optional. The various embodiments in this specification are described in a related manner, and the same or similar parts between the various embodiments refer to each other. In particular, for the device, equipment, and system embodiments, since they are basically similar to the method embodiments, the description is relatively simple, and the relevant parts refer to the partial description of the method embodiment.

[0185] The above-mentioned embodiments only express several implementation methods of the present invention, and the description thereof is relatively specific and detailed, but it cannot be understood as limiting the scope of patent protection. It should be pointed out that, for a person of ordinary skill in the art, several variations and improvements can be made without departing from the concept of the present invention, and these all belong to the scope of protection of the present invention. Therefore, the scope of protection of the present invention shall be subject to the attached claims.

Claims

1. A chemical chaining gasification method for iron-rich sludge, characterized in that: include: The iron-rich sludge is subjected to filter pressing and crushing treatment in sequence to generate iron-rich sludge particles with a moisture content of 40% to 50%, wherein the diameter of the iron-rich sludge particles ranges from 0.5 mm to 1 mm; Passing the iron-based oxygen carrier and the iron-rich sludge particles into a fluidized bed reactor for a chemical chain gasification reaction, so that the iron-rich sludge particles are ashed to generate supplementary oxygen carriers during the chemical chain gasification reaction; Performing the chemical chain gasification reaction based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone the chemical chain gasification reaction; After the chemical chain gasification reaction is carried out based on the supplementary oxygen carrier, the iron-based oxygen carrier and the iron-rich sludge particles that have not undergone the chemical chain gasification reaction, the method further includes: The air inlet atmosphere of the fluidized bed reactor is switched to air, the sludge ash generated by the chemical chaining gasification reaction is crushed, floated and discharged, and the iron-based oxygen carrier and the sludge ash supplementary oxygen carrier particles are regenerated to complete a chemical chaining gasification cycle of iron-rich sludge.

2. The method according to claim 1, characterized in that The iron-based oxygen carrier includes at least one of the following: a copper-iron spinel oxygen carrier, a perovskite-type oxygen carrier and a sludge ash-formed oxygen carrier.

3. The method according to claim 2, characterized in that The molecular formula of the copper iron spinel oxygen carrier is CuFe2O4, and the molecular formula of the perovskite oxygen carrier is CaMn 0.5 Fe 0.5 O 3-δ .

4. The method according to claim 2, characterized in that: The copper-iron spinel oxygen carrier is obtained based on the following method: The red mud is subjected to a crushing treatment, a drying treatment and a sieving treatment in sequence to obtain a red mud powder, wherein the particle size of the red mud powder is less than 75 μm, the drying temperature of the drying treatment is 105 degrees Celsius, and the drying time is 4 hours; The red mud powder, copper oxide and water are mixed to generate a first mixture, wherein the water content of the first mixture is 10% to 15%, and the mass ratio of the red mud powder to the copper oxide is 17:3; The first mixture is subjected to sequential balling, shade drying and baking treatments to obtain the copper-iron spinel oxygen carrier.

5. The method according to claim 4, characterized in that The first mixture is subjected to sequential balling, shade drying and drying to obtain the copper-iron spinel oxygen carrier, comprising: The first mixture is pelletized to generate a first mixture pellet, wherein the particle size of the first mixture pellet is 0.5 mm to 1 mm; Placing the first mixture ball blank in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the first mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours; Based on a first preset drying condition, placing the first mixture ball blank after the shade drying process in a drying device for drying process to obtain the copper-iron spinel oxygen carrier; The first preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping the temperature for 2 hours, and then heating the drying device to 900 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping the temperature for 6 hours.

6. The method according to claim 2, characterized in that The perovskite-type oxygen carrier is obtained based on the following method: The red mud, manganese sand and calcium hydroxide are respectively subjected to pulverization, drying and screening in sequence to obtain red mud powder, manganese sand powder and calcium oxide powder, wherein the particle sizes of the red mud powder, the manganese sand powder and the calcium oxide powder are less than 75 μm, the drying temperature of the drying treatment is 105 degrees Celsius, and the drying time is 4 hours; The red mud powder, the manganese sand powder, the calcium oxide powder and water are mixed to generate a second mixture, wherein the water content of the second mixture is 10% to 15%, and the mass ratio of the red mud powder, the manganese sand powder and the calcium oxide powder is 36:38:26; The second mixture is subjected to sequential balling, shade drying and baking treatments to obtain the perovskite-type oxygen carrier.

7. The method according to claim 6, characterized in that The second mixture is subjected to sequential balling, shade drying and drying to obtain the perovskite-type oxygen carrier, comprising: The second mixture is pelletized to generate a second mixture pellet, wherein the particle size of the second mixture pellet is 0.5 mm to 1 mm; Placing the second mixture ball blank in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the second mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours; Based on the second preset drying condition, placing the second mixture pellet after the shade drying process in a drying device for drying process to obtain the perovskite type oxygen carrier; The second preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping the temperature for 2 hours, and then heating the drying device to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping the temperature for 6 hours.

8. The method according to claim 2, characterized in that: The sludge ash shaped oxygen carrier is obtained based on the following method: The iron-rich sludge is crushed and dried in sequence to obtain sludge particles, wherein the drying temperature of the drying process is 105 degrees Celsius and the drying time is 4 hours; The sludge particles are subjected to ash treatment and sieving treatment in sequence to obtain sludge ash powder, wherein the particle size of the sludge ash powder is less than 75 μm; mixing the sludge ash powder and water to obtain a third mixture; The third mixture is subjected to sequential pelletizing, shade drying and oven drying processes to obtain the sludge ash shaped oxygen carrier.

9. The method according to claim 8, characterized in that The third mixture is subjected to sequential pelletizing, shade drying and drying to obtain the sludge ash shaped oxygen carrier, comprising: The third mixture is pelletized to generate a third mixture pellet, wherein the pellet has a particle size of 0.5 mm to 1 mm; Placing the third mixture ball blank in an environment of 20 degrees Celsius to 30 degrees Celsius for shade drying to obtain the third mixture ball blank after shade drying, wherein the shade drying time includes 24 hours to 48 hours; Based on the third preset drying condition, placing the third mixture pellet after the shade drying process in a drying device for drying process to obtain the sludge ash shaped oxygen carrier; The third preset drying condition includes: heating the drying device to 350 degrees Celsius at a heating rate of 5 degrees Celsius per minute, keeping the temperature for 2 hours, and then heating the drying device to 850 degrees Celsius at a heating rate of 5 degrees Celsius per minute, and keeping the temperature for 6 hours.

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