Waste coal water slurry compounding method with sulfate salt hazardous waste replacing alkali and application thereof

Abstract

The application discloses a waste water coal slurry compounding method with sulfate hazardous waste instead of alkali and application thereof, and the water coal slurry compounding comprises the following steps: (a) detecting and calculating the mass percentage of Na + , K + , Cl ‑ , Br ‑ , F ‑ and SO4 2‑ in various inorganic salt-containing hazardous wastes; (b) detecting and calculating the mass percentage of Cl, Br and F in various halogen-containing organic wastes; (c) selecting the inorganic salt-containing hazardous waste and the halogen-containing organic waste, and mixing uniformly after being measured according to n1 / n2=alpha; n1 is the sum of the amounts of substances of Na + , K + in the inorganic salt-containing hazardous waste and Cl ‑ , Br ‑ and F ‑ , n2 is the sum of the amounts of substances of Cl, Br and F in the halogen-containing organic waste, and alpha is controlled to be 1.05-1.15; and (d) mixing the premix with raw material coal to prepare slurry. The application reduces the amount of alkali, expands the disposal outlet of waste salt, and can effectively reduce the corrosive harm of halogen to the furnace bricks of a gasifier.

Description

Technical Field

[0001] This invention relates to the field of hazardous waste resource utilization technology, and in particular to a waste-water-coal slurry formulation method and its application using sulfate hazardous waste as a substitute for alkali. Background Technology

[0002] Hazardous waste refers to waste that is listed in the National Hazardous Waste List or identified as having hazardous characteristics according to the national hazardous waste identification standards and methods. It has six major characteristics: corrosiveness, toxicity, flammability, reactivity, infectivity, and danger. Only qualified disposal units that have been approved and issued a "Hazardous Waste Operation License" by the provincial-level ecological and environmental department can dispose of waste within the scope of the license.

[0003] 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.

[0004] Waste salts often exist in mixed form, originating from various waste-generating units. Inorganic salts are mainly NaCl and Na2SO4, while organic salts are often related to organic intermediates from pharmaceutical and chemical enterprises, such as halogenated organic compounds. If waste salts are treated using coal-water slurry technology, the organic salts will rapidly decompose during the gasification stage, easily forming acidic gases. These gases then dissolve in water during subsequent rapid cooling, forming acids or easily soluble acidic salts. Therefore, it is necessary to add an appropriate amount of alkali to the coal-water slurry before gasification to control the generation of acidic gases during the gasification stage and reduce the corrosive damage of halogens to the gasifier bricks. However, alkali is expensive, which is not conducive to cost control. If inorganic sulfates can replace alkali in the co-treatment of organic waste salts, it can not only reduce the amount of alkali used and control costs, but also expand the disposal options for waste salts and reduce acid formation during the gasification reaction, effectively reducing the corrosive damage of halogens to the gasifier bricks. Summary of the Invention

[0005] The purpose of this invention is to overcome the shortcomings of the prior art and provide a waste-water-coal slurry formulation method and its application using sulfate hazardous waste as a substitute for alkali.

[0006] To achieve the above objectives, the present invention adopts the following technical solution:

[0007] A method for preparing waste-water-coal slurry using sulfate hazardous waste as a substitute for alkali includes the following steps:

[0008] (a) Various hazardous wastes containing inorganic salts were classified and stored separately, and the Na content in each type of hazardous waste was tested and calculated. + K + Cl-, Br - F - SO4 2- The mass percentage content; hazardous waste containing inorganic salts is divided into hazardous waste containing sulfates and hazardous waste containing halides;

[0009] (b) Detect and calculate the mass percentage of Cl, Br, and F in various halogenated organic wastes;

[0010] (c) Select at least one sulfate-containing hazardous waste and at least one halogen-containing organic waste, and select or not select at least one halide-containing hazardous waste, measure and mix them evenly according to the formula (I) to obtain a premix;

[0011] n1 / n2 = α(I)

[0012] In formula (I), n1 represents the Na content in the hazardous waste containing inorganic salts. + K + The sum of the amounts of substance and Cl - ,Br - F - The difference in the sum of the amounts of substances, n2 is the sum of the amounts of Cl, Br, and F in halogen-containing organic waste, and α is controlled between 1.05 and 1.15;

[0013] (d) The premixed material after the compatibility calculation is fed into the grinding device with the raw coal in proportion to make a slurry, thereby obtaining a coal-water slurry.

[0014] It also includes step (e): transporting the coal-water slurry prepared in step (d) to an intermediate tank for further maturation and stirring.

[0015] Sulfate-containing hazardous waste refers to hazardous waste whose main components are Na2SO4 or K2SO4.

[0016] In step (d), the mass ratio of the premix to the raw coal is 1.5-10, and the concentration of the coal-water slurry is controlled at 55-64 wt%.

[0017] An application of a waste-water-coal slurry formulation method that uses sulfate hazardous waste to replace alkali involves pressurizing the slurry with a high-pressure pump, then simultaneously injecting the matured waste-water-coal slurry and pure oxygen into a gasifier at approximately 1300-1400°C. The slurry is rapidly atomized and gasified. Through direct heat exchange between the ultra-high temperature liquid slag discharge and the quench water, a phase change is completed within 1.6 seconds, forming harmless glassy slag, halogen salts, and resource-based gases containing Cl, H2S, and H2. The halogen salts dissolve in the black water and enter the circulating water system.

[0018] The steam produced by the gasification heat exchange process of coal-water slurry is used as a heat source for the evaporation and crystallization of halogen salts in the circulating water system to produce industrial by-product salts; H2S is fed into the desulfurization section along with the resource recovery gas and refined into industrial by-product sulfur.

[0019] The resulting black water pH was controlled at 6-8.

[0020] The beneficial effects of this invention are:

[0021] 1. The co-treatment of organic waste salts with inorganic sulfates expands the disposal options for waste salts;

[0022] 2. After the waste material is atomized and dispersed, the coal-water slurry undergoes rapid gasification reaction. Hazardous waste containing sulfate and other hazardous wastes have the same probability of competing for the opportunity to react with oxygen. Sulfate ions are converted into H2S and enter the gas phase, reducing the chance of anions in the slurry forming acidic gases that are easily soluble in water.

[0023] 3. Make full use of the anions SO4 in saline hazardous waste 2- The excess cations after being reduced to H2S combine with halogens produced by the decomposition of organic matter, thereby reducing the need for additional alkali to adjust the pH after halogens combine with hydrogen.

[0024] 4. Controlling and reducing acid formation during the gasification reaction effectively reduces the corrosive damage of halogens to the gasifier bricks. Attached Figure Description

[0025] Figure 1 This is a structural diagram of the improved grinding apparatus of the present invention;

[0026] Figure 2 for Figure 1 Enlarged view of point A in the middle;

[0027] Figure 3 for Figure 1 Enlarged view of point B in the middle;

[0028] Figure 4 for Figure 1 Enlarged view of point C in the middle.

[0029] In the diagram: A. Cauldron body 1, First grinding assembly 2, A. Rotating shaft 21, Telescopic rod 22, Connector 23, Through hole 231, Partition 3, Slide groove 31, Cylinder 32, Sealing plate 4, B. Cauldron body 5, Discharge pipe 51, Second grinding assembly 6, B. Rotating shaft 61, Grinding rod 62, Rod body 621, Through hole 6211, Flange 6212, Limiting part 622, Ring limiting part 6221, Horizontal joint part 6222, Abutting flange 6223, Steel ball 623, Connector 63, Through hole 631, Motor 7. Detailed Implementation

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

[0031] This invention relates to a waste-water-coal slurry formulation method that uses sulfate hazardous waste as a substitute for alkali, comprising the following steps:

[0032] (a) Various hazardous wastes containing inorganic salts were classified and stored separately, and the Na content in each type of hazardous waste was tested and calculated. + K + Cl - ,Br - F - SO4 2- The percentage content by mass. Among them, hazardous waste containing inorganic salts is divided into hazardous waste containing sulfates and hazardous waste containing halides; hazardous waste containing sulfates is hazardous waste with Na2SO4 or K2SO4 as the main component.

[0033] (b) Detect and calculate the mass percentage of Cl, Br, and F in various halogenated organic wastes;

[0034] (c) Select at least one sulfate-containing hazardous waste and at least one halogen-containing organic waste, and select or not select at least one halide-containing hazardous waste, measure and mix them evenly according to the formula (I) to obtain a premix;

[0035] n1 / n2 = α(I)

[0036] In formula (I), n1 represents the Na content in the hazardous waste containing inorganic salts. + K + The sum of the amounts of substance and Cl - ,Br - F - The difference in the sum of the amounts of substances, n2 is the sum of the amounts of Cl, Br, and F in halogen-containing organic waste, and α is controlled between 1.05 and 1.15;

[0037] (d) The premixed material, after compatibility calculation, is fed into a grinding device with raw coal in a certain proportion to prepare a coal-water slurry. The mass ratio of the premixed material to the raw coal is 1.5-10; the concentration of the coal-water slurry is controlled at 55-64 wt%. Hazardous waste containing inorganic salts or halogenated salts contains water. The concentration of the coal-water slurry is controlled by adjusting the proportion of these two types of hazardous waste, and water can be added as needed.

[0038] (e) The coal-water slurry prepared in step (d) is transferred to an intermediate tank for further maturation and stirring. The resulting coal-water slurry particle size distribution is controlled as follows: ≤200 mesh 45-50%, ≤20 mesh 98-100%, and ≤14 mesh 100%.

[0039] This invention relates to a waste-water-coal slurry formulation method that uses sulfate hazardous waste as a substitute for alkali, applicable to the resource-based treatment and utilization of hazardous waste. Specifically, after pressurization by a high-pressure slurry pump, the matured coal-water slurry and pure oxygen are simultaneously injected into a gasifier at 1300-1400℃. Rapid atomization and gasification occur, followed by direct heat exchange between the ultra-high temperature liquid slag discharge and quench water, completing a phase change within 1.6 seconds. This results in harmless glassy slag, halogen salts, and resource-based gases containing Cl (specifically CO and CO2), H2S, and H2. The halogen salts dissolve in black water (pH 6-8) and enter the circulating water system. The byproduct steam from the coal-water slurry gasification heat exchange process is used as a heat source for the evaporation and crystallization of the halogen salts in the circulating water system, producing industrial byproduct salts. H2S, along with the resource-based gases, enters the desulfurization section for refining into industrial byproduct sulfur. In this application, SO4 in the system... 2- It is converted into H2S and enters the gas phase, carrying away H. + Avoid SO4 2- The generation of acid also effectively reduces the chance of halogens forming acid, thus significantly reducing the amount of alkali needed for subsequent black water pH adjustment, or even eliminating the need for alkali replenishment. It also reduces the corrosive damage of hydrogen halides to the gasifier bricks and subsequent pipelines. The halogen salts are partly derived from inorganic waste salts and partly from hydrogen halides produced by the cracking of halogen-containing organic matter and metal cations in the system (due to SO4). 2- The excess metal cations produced during the conversion are combined to form the gasifier. The ratio of the volumetric flow rate of the coal-water slurry to the volumetric flow rate of the oxygen feed is controlled at 460-500 (this value is calculated based on an oxygen-to-carbon atomic ratio of 0.95-1.0, and finally converted into the oxygen-to-coal slurry volume ratio). It varies slightly depending on the carbon content of the raw coal, the concentration of the coal-water slurry, and the purity of the oxygen. The preferred volume ratio is 485.

[0040] This invention relates to a waste-water-coal slurry formulation method and its application using sulfate hazardous waste as a substitute for alkali. Specific embodiments are as follows:

[0041] Example 1

[0042] (a) Various salt-containing hazardous wastes were classified and stored separately. Sodium sulfate hazardous waste was selected, and its sodium content (Na) was determined by ICP. + The concentration was 30.46 wt%, and the chlorine content was determined by ion chromatography to be (Cl... - 10.37wt% sulfate content (SO4) 2- The content was 49.54 wt%.

[0043] (b) The chlorine content of the chlorinated organic waste was determined to be 1.03 wt% by liquid chromatography;

[0044] (c) Through slurry formation tests and compatibility calculations, sodium sulfate hazardous waste and chlorine-containing organic waste are measured and mixed evenly according to the formula n1 / n2=α to obtain a premix; where n1 is the Na content in the sodium sulfate hazardous waste. + Amount of substance and Cl - The difference in the amount of substance, n2 is the amount of Cl in the chlorinated organic waste. Calculations show that, with 0.8 tons of sodium sulfate hazardous waste and 27.1 tons of chlorinated organic waste, α = (30.46% × 0.8 / 23 - 10.37% × 0.8 / 35.5) / (1.03% × 27.1 / 35.5) = 1.05.

[0045] (d) The premixed material and raw coal (the mass ratio of premixed material to raw coal is 3) were fed into the grinding device for pulping; the concentration of coal-water slurry was measured to be 56.8%.

[0046] (e) The coal-water slurry prepared in step (d) is sent to an intermediate tank for further maturation and stirring for 2 hours.

[0047] (f) After being pressurized by a high-pressure slurry pump, the matured coal-water slurry and pure oxygen are simultaneously injected into a gasifier at 1370℃ (the ratio of the volumetric flow rate of the coal-water slurry to the volumetric flow rate of the oxygen in the gasifier is 485). Rapid atomization and gasification occur, and through direct heat exchange with ultra-high temperature liquid slag discharge and quench water, a phase change is completed within 1.6 seconds, forming harmless glassy slag, sodium chloride, and resource-recovered gases containing Cl (i.e., CO, CO2), H2S, and H2. In this step, SO4... 2- It is transformed into H2S, becoming a resource-based gas, and then refined into industrial by-product sulfur in the desulfurization process; Na + With sodium sulfate hazardous waste Cl - The chlorine produced by the decomposition of organic matter combines with the sodium chloride, which dissolves in the black water (the black water is controlled at pH=7.2) and enters the circulating water system.

[0048] (g) The by-product steam from the heat exchange process in step (f) is used as a heat source for the evaporation and crystallization of halogen salts in the circulating water system to produce 0.55 tons of sodium chloride industrial by-product salt; the resource-based gas is input into the desulfurization section to refine H2S into industrial by-product sulfur.

[0049] Example 2

[0050] (a) Various salt-containing hazardous wastes were classified and stored separately. Sodium sulfate hazardous waste and potassium sulfate hazardous waste were selected. The sodium content (Na) in the sodium sulfate hazardous waste was determined by ICP. + The concentration was 30.46 wt%, and the chlorine content was determined by ion chromatography to be (Cl... - 10.37wt% sulfate content (SO4) 2- The potassium content (K) in the potassium sulfate hazardous waste was 49.54 wt%; the potassium content (K) was determined by ICP. + The concentration was 40.35 wt%, and the chlorine content was determined by ion chromatography to be (Cl... - 6.65wt%, sulfate content (SO4) 2- The content was 40.67 wt%.

[0051] (b) The chlorine content of the chlorinated organic waste was determined to be 1.52 wt% by liquid chromatography;

[0052] (c) Through slurry-forming tests and compatibility calculations, sodium sulfate hazardous waste, potassium sulfate hazardous waste, and chlorine-containing organic waste are measured according to the formula n1 / n2=α and then mixed evenly to obtain a premix; where n1 is the Na content in sodium sulfate hazardous waste and potassium sulfate hazardous waste. + K + The amount of substance and Cl - The difference in the amount of substance, n2 is the amount of Cl in the chlorinated organic waste. Calculations show that, with 0.5 tons of sodium sulfate hazardous waste, 0.5 tons of potassium sulfate hazardous waste, and 20.3 tons of chlorinated organic waste, α = (30.46% × 0.5 / 23 + 40.35% × 0.5 / 39 - 10.37% × 0.5 / 35.5 - 6.65% × 0.5 / 35.5) / (1.52% × 20.3 / 35.5) = 1.081.

[0053] (d) The premixed material and raw coal (mass ratio of premixed material to raw coal is 4.8) were fed into the grinding device for pulping; the concentration of waste coal-water slurry was measured to be 55.3%;

[0054] (e) The coal-water slurry prepared in step (d) is sent to an intermediate tank for further maturation and stirring for 2 hours;

[0055] (f) After being pressurized by a high-pressure slurry pump, the matured coal-water slurry and pure oxygen are simultaneously injected into a gasifier at 1380℃ (the ratio of the volumetric flow rate of the coal-water slurry to the volumetric flow rate of the oxygen in the gasifier is 490). Rapid atomization and gasification occur, and through direct heat exchange with ultra-high temperature liquid slag discharge and quench water, a phase change is completed within 1.6 seconds, forming harmless glassy slag, sodium chloride, and resource-recovered gases containing Cl (i.e., CO, CO2), H2S, and H2. In this step, SO4... 2- It is transformed into H2S, becoming a resource-based gas, and then refined into industrial by-product sulfur in the desulfurization process; Na + With sodium sulfate hazardous waste Cl - Cl in potassium sulfate hazardous waste - The chlorine produced by the decomposition of organic matter combines with the sodium chloride, which dissolves in the black water (the black water is controlled at pH=7.4) and enters the circulating water system.

[0056] (g) The by-product steam from the heat exchange process in step (f) is used as a heat source for the evaporation and crystallization of halogen salts in the circulating water system to produce 0.33 tons of sodium chloride industrial by-product salt; the resource-based gas is input into the desulfurization section to refine H2S into industrial by-product sulfur.

[0057] Example 3

[0058] (a) Various types of saline hazardous waste were classified and stored separately. Potassium sulfate hazardous waste was selected, and its potassium content (K) was determined by ICP. + The concentration of chlorine was 37.43 wt%, and the chlorine content was determined by ion chromatography to be (Cl...). - 5.65%, bromine content (Br) - 0.22wt% sulfate content (SO4) 2- The content was 38.3 wt%.

[0059] (b) The chlorine content of the chlorinated organic waste was determined to be 1.44 wt% by liquid chromatography;

[0060] (c) Through slurry-forming tests and compatibility calculations, potassium sulfate hazardous waste and chlorine-containing organic waste are measured according to the formula n1 / n2=α and then mixed evenly to obtain a premix; where n1 is the potassium sulfate hazardous waste containing K + Amount of substance and Cl - ,Br - The difference between the amounts of substances, n2, represents the amount of Br in the chlorinated organic waste. Calculations show that, with 0.5 tons of potassium sulfate hazardous waste and 8.7 tons of chlorinated organic waste,

[0061] α=(37.43%×0.5 / 39-5.65%×0.5 / 35.5-0.22%×0.5 / 79.9) / (1.44%×8.7 / 35.5)=1.14.

[0062] (d) The premixed material and raw coal (the mass ratio of premixed material to raw coal is 2) were fed into the grinding device for pulping; the concentration of waste coal-water slurry was measured to be 54.7%;

[0063] (e) The coal-water slurry prepared in step (d) is sent to an intermediate tank for further maturation and stirring for 2 hours;

[0064] (f) After being pressurized by a high-pressure slurry pump, the matured coal-water slurry and pure oxygen are simultaneously injected into a gasifier at 1400℃ (the ratio of the volumetric flow rate of the coal-water slurry to the volumetric flow rate of the oxygen in the gasifier is 500). Rapid atomization and gasification occur, and through direct heat exchange with ultra-high temperature liquid slag discharge and quench water, a phase change is completed within 1.6 seconds, forming harmless glassy slag, potassium chloride, and resource-recovered gases containing Cl (i.e., CO, CO2), H2S, and H2. In this step, SO4... 2- It is transformed into H2S, becoming a resource-based gas, and then refined into industrial by-product sulfur in the desulfurization process; K + Cl in potassium sulfate hazardous waste - It combines with chlorine produced by the decomposition of organic matter to become potassium chloride, which dissolves in black water (black water is controlled at pH=7.5) and enters the circulating water system.

[0065] (g) The by-product steam from the heat exchange process in step (f) is used as a heat source for the evaporation and crystallization of halogen salts in the circulating water system to produce 0.291 tons of potassium chloride industrial by-product salt; the resource-based gas is input into the desulfurization section to refine H2S into industrial by-product sulfur.

[0066] Examples 4-6

[0067] Studies have shown that appropriately increasing the concentration of coal-water slurry can effectively improve the gasification efficiency and reduce the energy consumption (coal and oxygen consumption) of the gasification reaction. A reasonable particle size distribution of pulverized coal can fill the gaps between large particles with smaller particles, reducing the water content in the gaps and thus increasing the slurry concentration. However, relying solely on traditional ball mills or rod mills to grind coal-water slurry makes it difficult to obtain a slurry with a more reasonable particle size distribution.

[0068] This invention employs an improved grinding apparatus and conducts experiments according to the methods of Examples 1-3, denoted as Examples 4-6 (Examples 1-3 all use existing conventional rod mills). Figures 1-4As shown, the improved grinding device includes a coarse grinding mechanism and a fine grinding mechanism arranged vertically. The coarse grinding mechanism includes a transverse A-type vessel body 1, a first grinding component 2 rotatably disposed within the A-type vessel body 1, and a partition 3 that is sealed and slidably disposed within the A-type vessel body 1 and divides the A-type vessel body 1 into two chambers. The first grinding component 2 includes a rotating shaft 21 that rotatably passes through the A-type vessel body 1 and circumferentially distributed telescopic rods 22. One end of the telescopic rod 22 is fixedly connected to the rotating shaft 21, and the other end of the telescopic rod 22 is circumferentially slidably connected to the partition 3. The movement of the partition 3 causes the telescopic rods 22 to extend and retract. The fine grinding mechanism includes a transverse B-type vessel body 5 and a second grinding component 6 rotatably disposed within the B-type vessel body 5. The second grinding component 6 includes a pair of B-type rotating shafts 61 and a... The grinding rod 62, which is rotated by the B rotating shaft 61, includes a rod body 621, limiting members 622 fixed on both sides of the rod body 621, and steel balls 623 spaced along the rod body 621. The steel balls 623 pass through the rod body 621 and are limited on the rod body 621 by the limiting members 622. The steel balls 623 roll and abut against the rod body 621 and the limiting members 622. There are gaps between the steel balls 623 and the rod body 621 and the limiting members 622. The lower part of the A vessel body 1 is connected to the discharge pipe 51, and the discharge pipe 51 communicates with the inner cavity of the B vessel body 5. The partition 3 is connected to the sealing plate 4, which can move with the partition 3. The sealing plate 4 covers the opening of the discharge pipe 51 or makes the discharge pipe 51 communicate with the B vessel body 5.

[0069] The first grinding assembly 2 also includes a connector 23 fixed to a rotating shaft 21 located on the A vessel body 1. The rotating shaft 21 rotates through one side of the A vessel body 1. One end of the telescopic rod 22 is fixed to the connector 23, and the connector 23 has multiple through holes 231. The partition plate 3 has an annular groove 31 with a transverse T-shaped longitudinal section facing the telescopic rod 22. The other end of the telescopic rod 22 fits into the groove 31 and can slide around the groove 31. The connection between the transverse T-shaped annular groove 31 and the telescopic rod 22 ensures that the other end of the telescopic rod 22 will not detach from the groove 31 of the partition plate 3. It can slide within the groove 31 and can also be extended and retracted by the movement of the partition plate 3. The partition plate 3 is sealed to the inner wall of the A vessel body 1 by a sealing ring. The sealing ring is embedded around the perimeter of the partition plate 3, so that the partition plate 3 always remains sealed to the annular inner wall of the A vessel body 1 when sliding. The partition plate 3 can divide the A vessel body 1 into two sealed chambers. The partition 3 is driven to move by the cylinder 32. The telescopic rod 22 includes an inner rod part and an outer rod part that are slidably sleeved together. One end of the outer rod part is fixedly connected to the connector 23, and the other end of the outer rod part is slidably connected to the partition 3.

[0070] A pair of B-shafts 61 are respectively rotatably installed on both sides of the B-boiler body 5. The second grinding assembly 6 also includes a connector 63 located inside the B-boiler body 5 and fixedly connected to the pair of B-shafts 61 respectively. The connector 63 is provided with a plurality of through holes 631, and the grinding rod 62 is fixedly connected between the two connectors 63. The rod body 621 is plate-shaped, and multiple through holes 6211 are provided on the rod body 621. The inner wall of the through holes 6211 is raised to form circumferentially distributed flanges 6212. The limiting member 622 includes semi-circular annular limiting portions 6221 arranged in a row and transverse connecting portions 6222 connecting two adjacent annular limiting portions 6221. The transverse connecting portions 6222 are fixedly connected to the rod body 621 (fixed by fasteners). The inner wall of the annular limiting portion 6221 is provided with semi-circularly distributed abutting edges 6223. The steel balls 623 pass through the through holes 6211 one by one and abut against the flanges 6212 and abutting edges 6223. The flange 6212 of a limiting part 6221 and the abutting edge 6223 of a through hole 6211 cooperate to form a circumferential limit on the steel ball 623, so that the steel ball 623 will not detach from the rod body 621, and the gap formed between the steel ball 623 and the flange 6212 and between the steel ball 623 and the abutting edge 6223 can allow the coal-water slurry to pass through.

[0071] The annular inner wall of the B vessel 5 is corrugated, which is beneficial for grinding. The A rotating shaft 21 and the B rotating shaft 61 on one side are driven to rotate by the same motor 7.

[0072] When using the improved grinding device for pulping, the baffle 3 moves to bring the telescopic rod 22 into a retracted state, and the sealing plate 4 seals the outlet of the discharge pipe 51. The coal-water slurry is then fed into the B vessel 5 and the inner cavity of the A vessel 1 where the telescopic rod 22 is located. Figure 1 The inner cavity on the left side of the partition plate 3), the mass ratio of slurry 1 in vessel B 5 to vessel A 1:2, the first grinding component 2 and the second grinding component 6 rotate to grind the material; in vessel A 1, the material is ground through the gap between the telescopic rod 22 and the inner wall of vessel A 1, and the rotation of the telescopic rod 22 disperses and disperses the slurry, promoting grinding. The first grinding component 2 can grind the coal-water slurry material; in vessel B 5, the material is ground through the gap between the inner wall of vessel B 5 and the grinding rod 62, and the material is also ground between the steel ball 623 and the flange 6212, and between the steel ball 623 and the abutment flange 6223. The rotation of the grinding rod 62 also disperses and disperses the slurry, promoting grinding. The second grinding component 6 can achieve finer grinding of the coal-water slurry. Afterwards, the partition plate 3 is moved to make the telescopic rod 22 in a stretched state ( Figure 1The partition plate 3 is moved to the right to abut the end of vessel A 1, and the sealing plate 4 no longer seals the outlet of the discharge pipe 51. The slurry in vessel B 5 flows into vessel A 1, and under the stirring and grinding of the first grinding component 2, the materials in vessel A 1 and vessel B 5 are mixed evenly. The improved grinding device of this invention results in a more reasonable particle size distribution of the coal-water slurry, increasing the slurry concentration. Experiments show that, compared to examples 1-3, examples 4-6 ultimately achieved coal-water slurry concentrations increased by 5.01%, 4.86%, and 5.07%, respectively; gasification efficiencies increased by 4.95%, 4.73%, and 5.02%, respectively; and oxygen consumption decreased by 6.22%, 5.93%, and 6.31%, respectively. Furthermore, the particle size distribution of the coal-water slurry obtained in examples 1-6 all met the standards of ≤200 mesh accounting for 45-50%, ≤20 mesh accounting for 98-100%, and ≤14 mesh accounting for 100%.

[0073] 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 waste coal water slurry compounding method with sulfuric acid salt hazardous waste instead of alkali, characterized by, Includes the following steps: (a) Various types of hazardous waste containing inorganic salts were classified and stored separately, and the Na content in each type of hazardous waste containing inorganic salts was tested and calculated. + K + Cl - ,Br - F - SO4 2- The mass percentage content; hazardous waste containing inorganic salts is divided into hazardous waste containing sulfates and hazardous waste containing halides; (b) Calculate the mass percentage of Cl, Br, and F in various halogenated organic wastes; (c) Select at least one sulfate-containing hazardous waste, at least one halogen-containing organic waste, and select or not select at least one halide-containing hazardous waste, measure and mix them evenly according to the formula (I) to obtain a premix; n1 / n2 = α(I) In formula (I), n1 represents the Na content in the hazardous waste containing inorganic salts. + K + The sum of the amounts of substance and Cl - ,Br - F - The difference in the sum of the amounts of substances, n2 is the sum of the amounts of Cl, Br, and F in halogen-containing organic waste, and α is controlled between 1.05 and 1.15; (d) The premixed material after the compatibility calculation is fed into the grinding device with the raw coal in proportion to make a slurry, and the mass ratio of the premixed material to the raw coal is 1.5-10; The grinding device includes a coarse grinding mechanism and a fine grinding mechanism arranged vertically. The coarse grinding mechanism includes a horizontally arranged A-type vessel body (1), a first grinding component (2) rotatably disposed within the A-type vessel body (1), and a partition (3) that is sealed and slidably disposed within the A-type vessel body (1) and divides the A-type vessel body (1) into two chambers. The first grinding component (2) includes a rotating shaft (21) that rotatably passes through the A-type vessel body (1) and circumferentially distributed telescopic rods (22). One end of the telescopic rod (22) is fixedly connected to the rotating shaft (21), and the extension... The other end of the telescopic rod (22) is circumferentially slidably connected to the partition plate (3). The movement of the partition plate (3) drives the telescopic rod (22) to extend and retract. The fine grinding mechanism includes a horizontally arranged B-type vessel body (5) and a second grinding component (6) rotatably disposed within the B-type vessel body (5). The second grinding component (6) includes a pair of B-type rotating shafts (61) and circumferentially distributed grinding rods (62) driven to rotate by the pair of B-type rotating shafts (61). The grinding rods (62) include a rod body (621) and grinding rods (62) respectively fixed to the rod body (621). The rod (621) has limiting members (622) on both sides and steel balls (623) spaced apart along the rod body (621). The steel balls (623) pass through the rod body (621) and are limited on the rod body (621) by the limiting members (622). The steel balls (623) roll and abut against the rod body (621) and the limiting members (622). There are gaps between the steel balls (623) and the rod body (621) and the limiting members (622). The rod body (621) is plate-shaped and has multiple through holes (623). 11) The inner wall of the through hole (6211) is raised to form a circumferentially distributed flange (6212). The limiting member (622) includes a row of semi-circular annular limiting portions (6221) and a transverse connecting portion (6222) connecting two adjacent annular limiting portions (6221). The inner wall of the annular limiting portion (6221) is provided with a semi-circularly distributed abutting edge (6223). The steel ball (623) passes through the through hole (6211) one by one and abuts against the flange (6212) and the abutting edge (6223). The lower part of the A vessel body (1) is connected to a discharge pipe (51), and the discharge pipe (51) is connected to the inner cavity of the B vessel body (5). A sealing plate (4) that can move with the partition plate (3) is connected to the partition plate (3). The sealing plate (4) seals the outlet of the discharge pipe (51) or connects the discharge pipe (51) to the B vessel body (5). During grinding, the mass ratio of slurry in vessel B (5) to vessel A (1) is 1:

2.

2. The method according to claim 1, wherein the waste coal water slurry is prepared by replacing the alkali with the sulfate hazardous waste. It also includes step (e): transporting the coal-water slurry prepared in step (d) to an intermediate tank for further maturation and stirring.

3. The method of claim 1, wherein the waste coal water slurry is prepared by replacing the alkali with the sulfate hazardous waste. Sulfate-containing hazardous waste refers to hazardous waste whose main components are Na2SO4 or K2SO4.

4. The waste-water-coal slurry formulation method using sulfate hazardous waste as a substitute for alkali as described in claim 1, characterized in that, In step (d), the concentration of coal-water slurry is controlled at 55-64 wt%.

5. The use of a waste coal water slurry compounding method with sulfuric acid salt hazardous waste instead of alkali according to any one of claims 1 to 4, characterized in that, After being pressurized by a high-pressure slurry pump, the matured coal-water slurry and pure oxygen are simultaneously injected into a gasifier at 1300-1400℃, where they are rapidly atomized and gasified. Through direct heat exchange between the ultra-high temperature liquid slag discharge and the quench water, a phase change is completed within 1.6 seconds, forming harmless glassy slag, halogen salts, and resource-based gases containing Cl, H2S, and H2. The halogen salts dissolve in the black water and enter the circulating water system.

6. The use of a waste coal water slurry preparation method with sulfuric acid salt hazardous waste instead of alkali according to claim 5, characterized in that, The steam produced by the gasification heat exchange process of coal-water slurry is used as a heat source for the evaporation and crystallization of halogen salts in the circulating water system to produce industrial by-product salts; H2S is fed into the desulfurization section along with the resource recovery gas and refined into industrial by-product sulfur.

7. The use of a waste coal water slurry preparation method with sulfuric acid salt hazardous waste instead of alkali according to claim 5, characterized in that, The resulting black water pH was controlled at 6-8.

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