Method for resource utilization of salt-containing hazardous waste by coal water slurry gasification

Abstract

The application discloses a method for gasifying and recycling salt-containing hazardous waste by using coal-water slurry, which comprises the following steps: (a) storing the salt-containing hazardous waste in a classified manner and detecting the salt content; (b) uniformly mixing the salt-containing hazardous waste in a proportioned manner to form a premix with balanced cations and anions; (c) preparing a coal-water slurry by mixing the premix with raw coal in a proportioned manner; (d) continuing to age the coal-water slurry; (e) performing a gasification reaction on the aged coal-water slurry to form harmless glassy slag, sodium salt and resource-containing gas, while generating black water and by-product steam; and (f) using the by-product steam as a heat source to perform evaporation and crystallization of the sodium salt, and converting H2S into sulfur. The application has wide applicability in recycling waste salt, can realize salt separation in a harmless process, has high resource utilization rate, and can effectively reduce the corrosive damage of halogen to the gasifier bricks and subsequent pipelines.

Description

Technical Field

[0001] This invention relates to the field of hazardous waste resource utilization technology, and in particular to a method for the resource utilization of saline hazardous waste through coal-water slurry gasification. Background Technology

[0002] The disposal of saline hazardous waste is a global challenge. For example, my country generates over 300 million cubic meters of high-salinity wastewater annually, resulting in over ten million tons of mixed saline hazardous waste. Most of this waste is not properly disposed of, placing immense pressure on the ecological environment. Among the saline hazardous waste generated by the pharmaceutical and chemical industries, sodium chloride and sodium sulfate are two of the most common waste salts, especially in wastewater from coal chemical and dye industries, which contains large quantities of mixed salts composed of sodium chloride and sodium sulfate. Because conventional evaporation and crystallization techniques cannot separate these mixed salts, their utilization value is low, and they often need to be disposed of as hazardous waste by qualified hazardous waste management companies.

[0003] In the separation and crystallization system and method for waste mixed salts described in patent CN201910626617.7, the waste sodium chloride and sodium sulfate mixed salts are first incinerated or pyrolyzed, and then the mixed salts are dissolved in a dissolving tank (the mass concentration of the mixed salts is controlled at 20-30%). After primary filtration by immersion membrane, multiple salt separation evaporation crystallizations and dilution nanofiltrations are performed, followed by evaporation crystallization. This involves multiple separations and repeatable crystallizations with strict limit control, making salt separation difficult.

[0004] In the resource utilization treatment method of industrial waste salt described in patent CN201911382913.3, a two-step pyrolysis method is adopted, which involves medium-temperature oxygen-free pyrolysis (<700℃) and oxygen-free melt pyrolysis (<1000℃). The pyrolysis residue obtained by screening the pyrolysis at different temperature ranges is sent to the salt production process to produce industrial salt. Both pyrolysis furnaces use electric heating, which consumes a lot of energy. The pyrolysis process can pyrolyze organic matter, but sulfates cannot be reduced under these conditions and cannot be further converted.

[0005] In patent CN201810580716.1, a method for treating and reusing waste mixed salt containing organic matter, the waste mixed salt is treated at high temperature, and the product is dissolved and filtered to obtain a concentrated mixed salt solution. The concentrated salt solution is used as a forward osmosis draw solution. During the forward osmosis process, the draw solution is diluted to obtain a draw solution. This diluted draw solution is selectively separated to obtain solutions with multiple ionic components. The solutions with different ionic components are respectively concentrated by forward osmosis using the draw solution to obtain corresponding concentrated ionic solutions. The concentrated solutions are then crystallized to obtain the corresponding crystalline salts. Due to the difficulty in separating the mixed salts during utilization, the process of selectively separating each ionic component is complex.

[0006] The harmless treatment of waste salt is the fundamental prerequisite for all resource utilization. None of the methods mentioned above can selectively separate mixed waste salt containing inorganic and organic waste salt during the initial harmless treatment phase. To enable the resource utilization of mixed waste salt, conventional technologies require various oxidation methods to remove inorganic matter, rendering the mixed salt harmless, followed by specialized salt separation for resource recovery. Among existing technologies for waste salt harmless treatment, high-temperature treatment is considered the most effective and feasible method for the harmless treatment of hazardous solid waste containing salt as a byproduct, as it significantly reduces waste salt volume and removes organic matter. However, the high-temperature pyrolysis gas generated during this process has high treatment costs, and the hydrogen halide gas produced during decomposition causes severe corrosion to equipment.

[0007] In conclusion, in order to promote the comprehensive utilization of resources and environmental protection, it is of great significance to transform waste salt from hazardous waste that needs to be harmlessly disposed of into raw materials that can be utilized as resources. Summary of the Invention

[0008] The purpose of this invention is to overcome the shortcomings of the prior art and provide a method for the resource utilization of saline hazardous waste through coal-water slurry gasification. This method has wide applicability to the types of waste salts that can be treated, can simultaneously separate salts during the harmless treatment process, has a high resource utilization rate, and can effectively reduce the corrosive hazards of halogens to the gasifier bricks and subsequent pipelines.

[0009] To achieve the above objectives, the present invention adopts the following technical solution:

[0010] A method for the resource utilization of saline hazardous waste through coal-water slurry gasification includes the following steps:

[0011] (a) Various types of hazardous waste containing salt were classified and stored separately, and the salt content by mass was tested for each type.

[0012] (b) Through pulping tests and compatibility calculations, various salt-containing hazardous wastes were measured in proportion and mixed evenly to form a premix with anion and cation balance;

[0013] (c) The premix and raw coal are fed into a grinding device in proportion to make pulp;

[0014] (d) The coal-water slurry prepared in step (c) is fed into an intermediate tank for further maturation and stirring;

[0015] (e) The matured coal-water slurry is pressurized by a high-pressure slurry pump and simultaneously injected into a gasifier at 1300-1400℃ along with pure oxygen, causing it to rapidly atomize and gasify. Through direct heat exchange between the ultra-high temperature liquid slag discharge and the quench water, a phase change is completed within 1.6-2 seconds, forming harmless glassy slag, sodium salts, and resource-based gases containing H2, CO, H2S, and CO2. At the same time, black water and by-product steam are generated; soluble salts dissolve in the black water and enter the circulating water system.

[0016] (f) Using the by-product steam from the heat exchange process in step (e) as a heat source, sodium salt in the circulating water system is evaporated and crystallized to obtain industrial by-product salt.

[0017] In step (a), the salt-containing hazardous waste is classified into halogen-containing waste salt, sodium-containing organic waste salt, sulfuric acid waste salt, calcium-containing waste salt, and aluminum-containing waste salt.

[0018] In step (b), the premix is ​​a combination of at least two of the following: halogenated waste salt, sodium-containing organic waste salt, sulfated waste salt, calcium-containing waste salt, and aluminum-containing waste salt.

[0019] In step (c), the mass ratio of the premix to the raw coal is 1.5-10, and the concentration of the coal-water slurry is 55-64 wt%.

[0020] In step (d), the pH of the black water is controlled at 6-8.

[0021] The resource-based gas obtained in step (e) is fed into the desulfurization section to refine H2S into industrial by-product sulfur.

[0022] The beneficial effects of this invention are:

[0023] 1. The method of the present invention can simultaneously treat various waste salts containing halogens, organic sodium salts, sulfates, calcium salts, aluminum salts, etc., which contain cations and anions, and has wide applicability to the types of waste salts treated in the resource recovery process.

[0024] 2. Through reasonable formulation and matching, salts can be simultaneously separated into gas, liquid and solid phases during the harmless treatment process, achieving single-phase salt separation in each phase (calcium salts, aluminum salts, etc. migrate to glassy slag, and are used in building materials after water washing; sulfate ions are converted into H2S and enter the gas phase, and are used to prepare industrial by-product sulfur through desulfurization and refining; sodium salts dissolve in black water and enter the circulating water system, and are used to produce industrial salt through evaporation and crystallization).

[0025] 3. Anionic SO4 in the coal-water slurry system 2- After being reduced to H2S, the excess cations in the system can combine with the halogens produced by the cracking of organic matter in the coal-water slurry, effectively reducing the corrosive hazards of the halogens produced by the cracking of organic matter to the gasifier bricks and subsequent pipelines. Attached Figure Description

[0026] Figure 1 This is a structural diagram of the mill apparatus of the present invention;

[0027] Figure 2 for Figure 1 Enlarged view of point A in the middle;

[0028] Figure 3 for Figure 1 Enlarged view of point B in the middle.

[0029] In the figure: 1. Cauldron body, 11. First cauldron section, 111. Liner plate, 112. Discharge pipe, 113. Divider, 12. Second cauldron section, 13. Third cauldron section, C gear, 131. Feed port cauldron section, 14. Cauldron cover, 2. Grinding assembly, 3. A connecting plate, 311. Through hole, 32. B connecting plate, 321. Flange, 33. Grinding rod, 33. End plate, 331. Connecting rod, 332. Grinding bead, 333. Rotating shaft, 34. Partition plate, 4. Gear assembly, 5. A gear, 51. B gear, 52. Gear ring, 53. Connecting shaft, 54. Frame, 6. Cylinder, 7. Motor, 8. D gear, 81. Detailed Implementation

[0030] The present invention will be further described below with reference to the accompanying drawings and specific embodiments:

[0031] The present invention relates to a method for the resource utilization of saline hazardous waste through coal-water slurry gasification, comprising the following steps:

[0032] (a) Various types of saline hazardous waste were classified and stored separately, and the salt content by mass was tested separately. These saline hazardous wastes were classified as halogenated waste salt, sodium-containing organic waste salt, sulfate waste salt, calcium-containing waste salt, and aluminum-containing waste salt. In practice, this involved testing the mass percentages of chloride, sulfate, calcium, aluminum, and sodium in each saline hazardous waste.

[0033] (b) Through slurry formation test and compatibility calculation, various salt-containing hazardous wastes are measured in proportion and mixed evenly to form a premix with anionic and cation balance; the premix is ​​a combination of at least two of the following: halogen-containing waste salt, sodium-containing organic waste salt, sulfuric acid waste salt, calcium-containing waste salt, and aluminum-containing waste salt.

[0034] (c) The premix and raw coal are fed into a grinding device in a certain proportion for slurry preparation; the mass ratio of premix to raw coal is 1.5-10, the concentration of coal-water slurry is 55-64 wt%, and the pH of coal-water slurry is 6.5-8. Hazardous waste containing inorganic salts and hazardous waste containing halide salts contains water; the concentration of coal-water slurry is controlled by adjusting the proportion of these two types of hazardous waste, and water can be added as needed.

[0035] (d) The coal-water slurry prepared in step (c) is fed into an intermediate tank for further maturation and stirring;

[0036] (e) The matured coal-water slurry is pressurized by a high-pressure slurry pump and simultaneously injected with pure oxygen into a gasifier at 1300-1400℃. This causes rapid atomization and gasification. Through direct heat exchange between the ultra-high temperature liquid slag discharge and the quench water, a phase change is completed within 1.6-2 seconds, forming harmless glassy slag, sodium salts, and resource-based gases containing H2, CO, H2S, and CO2. Simultaneously, black water and by-product steam are generated. The pH of the black water is controlled at 6-8. Soluble salts dissolve in the black water and enter the circulating water system. The resource-based gases are input into the desulfurization section, where H2S is refined into industrial by-product sulfur. The resource-based gases then enter the syngas system to produce high-purity hydrogen, liquid CO2, methanol, and other resource-based products.

[0037] (f) Using the by-product steam from the heat exchange process in step (e) as a heat source, sodium salt in the circulating water system is evaporated and crystallized to obtain industrial by-product salt.

[0038] The resource utilization method in this invention achieves the unification of salts in each phase and simultaneously realizes salt separation during the harmless treatment process. The three-phase salt separation process is as follows: ① Calcium salts, aluminum salts, etc., are separated to the solid phase to generate glassy slag for the building materials industry; ② Soluble salts such as sodium salts are separated to the aqueous phase (circulating water system) along with water from gasification quenching, and the salt is distilled using by-product steam to obtain by-product sodium chloride; ③ Sulfates are reduced to H2S through anoxic reduction and separated to the gas phase (resource-utilized gas), and then purified through desulfurization to prepare industrial by-product sulfur. In addition, after the anionic sulfate ions in the saline hazardous waste are reduced to H2S, the excess cations in the system can combine with the halogens produced by the cracking of organic matter in the coal-water slurry, reducing the corrosive hazards of halogens to the gasifier bricks and subsequent pipelines.

[0039] The specific implementation method is as follows:

[0040] Example 1

[0041] A method for the resource utilization of saline hazardous waste through coal-water slurry gasification includes the following steps:

[0042] (1) Various salt-containing hazardous wastes are classified and stored separately, and are classified as halogen-containing waste salt, sodium-containing organic waste salt, sulfuric acid waste salt, calcium-containing waste salt, and aluminum-containing waste salt;

[0043] Waste sodium chloride, waste sodium sulfate, and waste sodium acetate were selected. The sodium chloride waste salt was found to contain 32.47% sodium, 46.5% chloride, and 4.9% sulfate. The waste sodium sulfate waste salt was found to contain 49.3% sulfate, 23.62% sodium, 3.89% calcium, and 5.82% carbonate. The waste sodium acetate waste salt was found to contain 22.83% sodium and 58.6% acetate.

[0044] (2) Through slurry formation test and compatibility calculation, take 1 ton of sodium chloride waste salt, 0.2 tons of sodium sulfate waste salt and 1 ton of sodium acetate waste salt, mix them evenly, and compatibility form a premix with anion and cation balance;

[0045] (3) The premix and raw coal are fed into the grinding device for pulping by means of conveying and pumping through a tubular chain conveyor. The mass ratio of the premix to the raw coal is 2, the concentration of the coal-water slurry is 56.87 wt%, and the pH of the coal-water slurry is 7.2.

[0046] (4) The coal-water slurry prepared in step (c) is sent into an intermediate tank and stirred for 2 hours to mature.

[0047] (5) After the matured coal-water slurry is pressurized by a high-pressure slurry pump, it is simultaneously injected into a gasifier at 1350°C along with pure oxygen, so that it can be rapidly atomized and gasified. Through direct heat exchange between ultra-high temperature liquid slag discharge and quench water, the phase change is completed within 2 seconds, forming harmless glassy slag, sodium chloride and resource-based gas containing H2, CO, H2S and CO2. At the same time, black water and by-product steam are generated. The pH of the black water is controlled at 6.8. Sodium chloride dissolves in the black water and enters the circulating water system. The resource-based gas is input into the desulfurization section to refine H2S into industrial by-product sulfur. The resource-based gas is input into the syngas system to prepare high-purity hydrogen, liquid CO2, methanol and other resource-based products.

[0048] (6) Using the by-product steam from the heat exchange process in (5) as a heat source, sodium chloride in the circulating water system is evaporated and crystallized to produce 0.63 tons of industrial by-product sodium chloride.

[0049] Example 2

[0050] A method for the resource utilization of saline hazardous waste through coal-water slurry gasification includes the following steps:

[0051] (1) Various types of saline hazardous waste were classified and stored separately. The various types of saline hazardous waste were classified into halogen-containing waste salt, sodium-containing organic waste salt, sulfate waste salt, calcium-containing waste salt, and aluminum-containing waste salt. Sodium chloride waste salt, sodium sulfate waste salt, and sodium acetate waste salt were selected. The sodium chloride waste salt was found to contain 32.47% sodium, 46.5% chloride, and 4.9% sulfate. The sodium sulfate waste salt was found to contain 48.41% sulfate, 23.2% sodium, 3.67% aluminum, and 7.34% silicate. The sodium acetate waste salt was found to contain 22.83% sodium and the calculated acetate content was 58.6%.

[0052] (2) Through slurry formation test and compatibility calculation, take 1 ton of sodium chloride waste salt, 0.1 ton of sodium sulfate waste salt and 1 ton of sodium acetate waste salt, mix them evenly, and compatibility into a premix with anion and cation balance;

[0053] (3) The premix and raw coal are fed into the grinding device for pulping by means of conveying and pumping through a tubular chain conveyor. The mass ratio of premix to raw coal is 1.9, the concentration of coal-water slurry is 56.65 wt%, and the pH of coal-water slurry is 7.3.

[0054] (4) The coal-water slurry prepared in step (c) is sent into an intermediate tank and stirred for 2 hours to mature.

[0055] (5) After the matured coal-water slurry is pressurized by a high-pressure slurry pump, it is simultaneously injected into a gasifier at 1400℃ along with pure oxygen, so that it can be rapidly atomized and gasified. Through direct heat exchange between ultra-high temperature liquid slag discharge and quench water, the phase change is completed within 1.6s, forming harmless glassy slag, sodium chloride and resource-based gas containing H2, CO, H2S and CO2. At the same time, black water and by-product steam are generated. The pH of the black water is controlled at 7. Sodium chloride dissolves in the black water and enters the circulating water system. The resource-based gas is input into the desulfurization section to refine H2S into industrial by-product sulfur. The resource-based gas is input into the syngas system to prepare high-purity hydrogen, liquid CO2, methanol and other resource-based products.

[0056] (6) Using the by-product steam from the heat exchange process in (5) as a heat source, sodium chloride in the circulating water system is evaporated and crystallized to produce 0.62 tons of industrial by-product sodium chloride.

[0057] Examples 3-4

[0058] Particle size distribution is a key factor affecting the concentration of coal-water slurry. Optimizing particle size distribution to improve packing efficiency is an important way to increase the concentration of coal-water slurry, which in turn helps to improve gasification efficiency and reduce oxygen consumption. Currently, traditional rod mills or ball mills are commonly used for slurry preparation. However, due to the limitations of the mills, grinding can only be carried out in one direction, making it difficult to obtain coal-water slurry with a reasonable particle size distribution.

[0059] This invention improves the mill device. Using this improved mill device, and following the methods of Examples 1-2 (using conventional mill devices), the treatment of saline hazardous waste through coal-water slurry gasification is carried out, referred to as Examples 3-4. The improved mill device includes a horizontally rotating vessel body 1, a grinding assembly 3 rotating in the opposite direction to the vessel body 1, and a fixedly installed vessel cover 2 (the vessel cover 14 is fixedly mounted on the frame 6). The vessel body 1 includes a first vessel section 11, a second vessel section 12, and a third vessel section 13 with successively decreasing diameters. The vessel cover 2 seals the opening of the third vessel section 13, and the third vessel section 13 is circumferentially rotatably connected to the vessel cover 2. The inner cavity of the first vessel section 11 and the inner cavity of the second vessel section 12 are separated or connected by a movable partition 4. The grinding assembly 3 includes an A connecting plate 31 and a B connecting plate 32 spaced apart, connected to the A connecting plate 31. A set of grinding rods 33 connected to the B connecting plate 32 and a rotating shaft 34 fixedly connected to the A connecting plate 31. Both the A connecting plate 31 and the B connecting plate 32 have through holes 311. When the partition plate 4 separates the inner cavity of the first vessel section 11 from the inner cavity of the second vessel section 12, the B connecting plate 32 and the partition plate 4 are circumferentially rotatably connected (the surface of the B connecting plate 32 protrudes to form a hemispherical flange 321, which rotatably abuts against the partition plate 4). The set of grinding rods 33 includes several circumferentially evenly distributed rings. The rotating shaft 34 passes through the third vessel section 13 and is rotatably connected to the vessel cover section 2. The rotating shaft 34 and the third vessel section 13 are connected by a gear assembly 5 for forward and reverse rotation. The rotating shaft 34 is clearance-fitted to the end of the second vessel section 12 or connected by a ring of ball bearings.

[0060] The vessel body 1 also includes a feed inlet vessel section 14 that rotates through the frame 6. One end of the first vessel section 11 is connected to the second vessel section 12, and the other end of the first vessel section 11 is connected to the feed inlet vessel section 14. The annular inner wall of the first vessel section 11 is equipped with a wear-resistant liner 111. The first vessel section 11 is actually equivalent to the vessel body of a rod mill in the prior art. The other end of the first vessel section 11 serves as the feed end, and the lower part of the first vessel section 11 is connected to a discharge pipe 112.

[0061] An annular separator 113 is fixedly installed at the port of the first vessel section 11, which is connected to the second vessel section 12. The separator 4 and the separator 113 are sealed together to separate the inner cavity of the first vessel section 11 from the inner cavity of the second vessel section 12. The separator 4 is driven to move by a cylinder 7.

[0062] The gear assembly 5 includes an A gear 51 fixedly mounted on a rotating shaft 34, a B gear 52 evenly distributed around the outer ring of the A gear 51, and a gear ring 53 fixedly mounted on the inner wall of the third vessel section 13. The inner and outer rings of the A gear 51 and the gear ring 53 are concentrically distributed, and the B gear 52 meshes with both the A gear 51 and the gear ring 53. A C gear 131 is fixedly mounted on the outer wall of the third vessel section 13. The vessel body 1 is driven to rotate by a motor 8, which is connected to the C gear 131 via a D gear 81. The B gear 52 is rotatably connected to the vessel cover section 2 via a coupling shaft 54. The longitudinal section of the vessel cover section 2 is transversely U-shaped, and the vessel cover section 2 is sealed and rotatably connected to the outer wall of the third vessel section 13.

[0063] The second vessel section 12 has a transverse U-shaped longitudinal section with the opening facing the first vessel section 11. The rotating shaft 34 passes through the vessel wall of the second vessel section 12 and is connected by a plane bearing. The rotating shaft 34 and the vessel wall of the second vessel section 12 are also sealed by a sealing ring.

[0064] The grinding rod 33 includes a pair of end plates 331, circumferentially distributed connecting rods 332 connected between the pair of end plates 331, and a row of grinding beads 333 placed within the structure formed by the pair of end plates 331 and the multiple connecting rods 332; the grinding beads 333 roll and abut against the connecting rods 332 and the end plates 331, and the gap between the grinding beads 333 and the connecting rods 332 allows slurry to pass through. The pair of end plates 331 are respectively fixedly connected to connecting plate A 31 and connecting plate B 32.

[0065] The improved grinding device of this invention is used for pulp preparation. The partition 4 separates the first reactor 11 and the second reactor 12. The pulp is put into the first reactor 11 and the second reactor 12 respectively. The mass ratio of the pulp in the first reactor 11 and the second reactor 12 is 2:1. The first reactor 11 is filled with steel balls. The reactor body 1 is driven to rotate. The steel balls and the liner 111 in the first reactor 11 grind the pulp in the first reactor 11. After the reactor body 1 rotates, the grinding assembly 3 is driven to rotate in the opposite direction through the gear assembly 5. The pulp in the second reactor 12 is ground in both directions in the gap between the inner wall of the second reactor 12 and the grinding rod 33. At the same time, the pulp is ground between the two grinding balls 333 and between the grinding balls 333 and the connecting rod 332. The rotating grinding assembly 3 also has the function of stirring and dispersing the pulp. The grinding assembly 3 can grind the pulp more finely. After a period of grinding, the moving partition 4 connects the first reactor 11 and the second reactor 12, so that the slurry in the second reactor 12 and the first reactor 11 can be quickly and evenly mixed.

[0066] This invention improves the slurry concentration by using an improved grinding device. Experiments showed that, compared to Examples 1-2, Examples 3-4 resulted in 4.98% and 5.05% higher concentrations of the coal-water slurry, respectively; 5.01% and 5.09% higher gasification efficiencies, respectively; and 6.14% and 6.25% lower oxygen consumption, respectively. Furthermore, testing revealed that the particle size distribution of the coal-water slurry obtained in Examples 1-4 all met the standards of ≤200 mesh (45-50%), ≤20 mesh (98-100%), and ≤14 mesh (100%).

[0067] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A method for the resource utilization of saline hazardous waste through coal-water slurry gasification, characterized in that, Includes the following steps: (a) Various types of hazardous waste containing salt were classified and stored separately, and the salt content by mass was tested for each type. (b) Through slurry formation test and compatibility calculation, various salt-containing hazardous wastes are measured in proportion and mixed evenly to form a premix with anion and cation balance; the premix is ​​a combination of at least two of the following: halogen-containing waste salt, sodium-containing organic waste salt, sulfate waste salt, calcium-containing waste salt, and aluminum-containing waste salt. (c) The premix and raw coal are fed into a grinding device in a certain proportion for pulping; the mass ratio of premix to raw coal is 1.5-10, and the concentration of coal-water slurry is 55-64 wt%. (d) The coal-water slurry prepared in step (c) is fed into an intermediate tank for further maturation and stirring; (e) After the matured coal-water slurry is pressurized by a high-pressure slurry pump, it is simultaneously injected into a gasifier at 1300-1400℃ along with pure oxygen, so that it is rapidly atomized and gasified. Through direct heat exchange between the ultra-high temperature liquid slag discharge and the quench water, the phase change is completed within 1.6-2 seconds, forming harmless glassy slag, sodium salts and resource-based gases containing H2, CO, H2S and CO2. At the same time, black water and by-product steam are generated; soluble salts dissolve in the black water and enter the circulating water system. (f) Using the by-product steam from the heat exchange process in step (e) as a heat source, sodium salt in the circulating water system is evaporated and crystallized to obtain industrial by-product salt. The grinding device includes a frame (6), a vessel body (1) arranged in a horizontal rotation, a grinding assembly (3) arranged in the opposite direction to the vessel body (1), and a fixedly installed vessel lid (2). The vessel body (1) includes a first vessel section (11), a second vessel section (12), and a third vessel section (13) with successively decreasing diameters. The vessel lid (2) covers the opening of the third vessel section (13), and the third vessel section (13) is circumferentially rotatably connected to the vessel lid (2). The first vessel section (11) The inner cavity of the first vessel (12) is separated from or connected to the inner cavity of the second vessel (12) by a movable partition (4). The grinding assembly (3) includes an A connecting plate (31) and a B connecting plate (32) spaced apart, a set of grinding rods (33) connected between the A connecting plate (31) and the B connecting plate (32), and a rotating shaft (34) fixedly connected to the A connecting plate (31). Both the A connecting plate (31) and the B connecting plate (32) are provided with through holes (311). When the partition (4) separates the first vessel... When the inner cavity of part (11) is connected to the inner cavity of the second vessel part (12), the B connecting plate (32) and the partition plate (4) are circumferentially rotatably connected. A set of grinding rods (33) includes a plurality of evenly distributed rings. The grinding rods (33) include a pair of end plates (331), circumferentially distributed connecting rods (332) connecting the pair of end plates (331), and a row of grinding beads (333) placed within the structure formed by the pair of end plates (331) and the plurality of connecting rods (332). The grinding beads (333) roll against the connecting rod (332) and the end plate (331), and the gap between the grinding beads (333) and the connecting rod (332) allows the slurry to pass through; the rotating shaft (34) passes through the third reactor part (13) and is rotatably connected to the reactor cover part (2). The rotating shaft (34) and the third reactor part (13) are connected by a gear assembly (5) rotating in opposite directions. The rotating shaft (34) is clearance-fitted to the end of the second reactor part (12) or connected by a ring of balls. The lid (2) is fixed on the frame (6). The body (1) also includes a feed port (14) that rotates through the frame (6). One end of the first feed port (11) is connected to the second feed port (12), and the other end of the first feed port (11) is connected to the feed port (14). The annular inner wall of the first feed port (11) is equipped with a wear-resistant liner (111). The other end of the first feed port (11) serves as the feed end. The lower part of the first feed port (11) is connected to a discharge pipe (112). During pulping, the partition (4) separates the first reactor (11) and the second reactor (12). The pulp is put into the first reactor (11) and the second reactor (12) respectively. Steel balls are put into the first reactor (11). The reactor body (1) is driven to rotate. The steel balls and wear-resistant liner (111) in the first reactor (11) grind the pulp in the first reactor (11). After the reactor body (1) rotates, the grinding assembly (3) is driven to rotate in the opposite direction through the gear assembly (5). The pulp in the second reactor (12) is ground in both directions in the gap between the inner wall of the second reactor (12) and the grinding rod (33). At the same time, the pulp is ground between the two grinding balls (333) and between the grinding balls (333) and the connecting rod (332). After a period of grinding, the partition (4) is moved to connect the first reactor (11) and the second reactor (12) and mix the pulp in the second reactor (12) and the first reactor (11) evenly.

2. The method for resource utilization of saline hazardous waste through coal-water slurry gasification as described in claim 1, characterized in that, In step (e), the pH of the black water is controlled at 6-8.

3. The method for resource utilization of saline hazardous waste through coal-water slurry gasification as described in claim 1, characterized in that, The resource-based gas obtained in step (e) is fed into the desulfurization section to refine H2S into sulfur, an industrial byproduct.

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