A coal clean processing and upgrading system and an upgrading method thereof

Abstract

The present application belongs to the technical field of coal processing, and particularly relates to a quality upgrading method of a coal clean processing and quality upgrading system, which realizes purification and quality upgrading of wide-granularity high-chlorine coal by synergistic effect of ultrasonic energy field and gradient acid leaching, and realizes online monitoring and dynamic regulation and control of the quality upgrading process. Under the ultrasonic energy field, the cavitation effect generates strong shock waves and micro-jets, which have a strong impact on the high-chlorine coal, disperses the pore channels between the coal particles, enables effective contact of the solvent with the high-chlorine coal, and promotes migration of the chlorine element. In addition, by detecting the quality upgrading process, the optimal reaction parameters are obtained, which guarantee effective removal of the chlorine element. The present application processes the high-chlorine coal by combining the multi-stage acid leaching process, has a high removal rate of water-soluble chlorine ions, is more thorough in dechlorination, and the organic acid can be recycled, has an efficient and environmentally-friendly dechlorination effect, opens up a new path for high-value and resourceful utilization of the high-chlorine coal, and has a broad application prospect.

Description

Technical Field

[0001] This invention belongs to the field of coal processing technology, and specifically relates to a method for improving the quality of a clean coal processing and upgrading system. Background Technology

[0002] In recent years, with the in-depth development and utilization of coal resources, the output of high-chlorine coal has gradually increased. During coal combustion, the hazards of chlorine are mainly manifested in the corrosion and fouling of boiler equipment and pipelines. When the chlorine content in coal exceeds 0.25%, serious risks of equipment corrosion and fouling arise. The higher the chlorine content, the more significant the corrosion, posing a serious threat to the safe operation of boiler equipment and pipelines. During combustion, the chlorine in coal is converted into harmful gases such as hydrogen chloride (HCl), which are released into the atmosphere, causing pollution. These gases not only corrode the furnace body and flue gas purification equipment but may also lead to atmospheric fluoride pollution, damaging the ecological environment and seriously harming the health of animals and plants. Therefore, it is necessary to dechlorinate high-chlorine coal after mining to significantly reduce the chlorine content.

[0003] Currently, dechlorination methods include drying, oxidation-reduction, and membrane separation. Drying converts chlorine in coal samples into volatile chlorides, which are then volatilized through heating or reduced pressure. Oxidation-reduction uses oxidants and reductants to control the sublimation and deposition of chlorine, achieving dechlorination. Membrane separation utilizes specific membrane materials and technologies to selectively separate chloride ions from coal solutions based on their charge and size. However, drying is only suitable for chlorine-containing substances with low moisture content or specific forms, and its removal efficiency for dissolved chloride ions is low. Oxidation-reduction reduces the selectivity of the reaction when chlorine coexists with other pollutants (such as organic matter and heavy metals). Membrane separation suffers from reduced flux due to the easy clogging of membrane pores by suspended solids, colloids, or organic matter in wastewater. Therefore, all three methods exhibit overall low efficiency and incomplete dechlorination. Summary of the Invention

[0004] To address the problems existing in the prior art, the purpose of this invention is to provide a method for upgrading a clean coal processing system. This method combines a multi-stage acid leaching process to treat high-chlorine coal, achieving a high removal rate of water-soluble chloride ions, more thorough dechlorination, and allowing the organic acids to be recycled, resulting in a highly efficient and environmentally friendly dechlorination effect.

[0005] The technical solution of this invention is:

[0006] A method for upgrading coal in a clean coal processing system includes the following steps:

[0007] S1: First-stage acid leaching: Coal sample and organic acid are mixed at a liquid-to-solid ratio of 10mL / g-15mL / g to form a mixture of coal sample and organic acid; the mixture is then transported to a first-stage ultrasonic reactor for dechlorination reaction, with the ultrasonic reaction temperature set at 60℃-80℃, ultrasonic reaction power at 500W-1000W, and ultrasonic reaction time at 3min-20min; the ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time are adjusted in real time during the reaction process, and the chlorine removal rate is monitored in real time to determine the optimal reaction parameters for the period with the highest chlorine removal rate;

[0008] S2: Perform solid-liquid separation on the mixture after the reaction to obtain a first-stage acid leaching residue and a first-stage acid leaching solution;

[0009] S3: Second-stage acid leaching: The first-stage acid leaching residue and organic acid are slurried and mixed at a liquid-solid ratio of 9mL / g-14mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The mixture is then placed in a second-stage ultrasonic reactor for dechlorination reaction, and the reaction parameters of the second-stage ultrasonic reactor are set to the optimal reaction parameters obtained in step S1.

[0010] S4: Perform solid-liquid separation on the mixture after the reaction to obtain a second-stage acid leaching residue and a second-stage acid leaching solution;

[0011] S5: Subsequent processing: The second-stage acid leaching solution is returned to step S1 as an organic acid solvent to continue participating in the dechlorination reaction in the first-stage ultrasonic reactor. The second-stage acid leaching residue is washed with deionized water, collected, and dried to constant weight for subsequent analysis. After adding copper oxide to the first-stage acid leaching solution to precipitate, solid-liquid separation is performed. The separated precipitate is evaporated and crystallized to obtain cuprous chloride crystals. The separated filtrate is returned to step S3 as an organic acid solvent for recycling.

[0012] Preferably, the particle size of the coal sample participating in the dechlorination reaction is 0.5 mm to 13 mm.

[0013] Preferably, the organic acid is citric acid, ascorbic acid, or a mixture of citric acid and ascorbic acid, wherein the mixing ratio of citric acid and ascorbic acid is (1~2):(1~2).

[0014] Preferably, the concentration of the organic acid is 0.5 mol / L to 3 mol / L.

[0015] Preferably, the mechanical stirrer in the first-stage and second-stage ultrasonic reaction devices rotates at a speed of 200 r / min to 300 r / min.

[0016] Preferably, the ultrasonic frequency of the first-stage and second-stage ultrasonic reaction devices is set to 20kHz-40kHz, and the ultrasonic intensity is 1W / cm². 2-5W / cm 2 .

[0017] Preferably, the ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time are controlled according to the following formula:

[0018] ,

[0019] in, ,

[0020] Ae −E a / RT ,

[0021] =1+(1+k(Cl)),

[0022] In the formula, , , These are the adjustment factors for the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module over time, where 0 < <1, 0< <1, 0< <1; , , The weights of the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module are respectively. , for / / ,and ; a For power regulation slope, a >0; b The power control intercept represents the fundamental contribution at zero power. b ≥0; P This is the real-time power value; Ae −E a / RT For Arrhenius's formula, A Pre-exponential factor, A =10 9 ~10 13 s −1 , R This is the gas constant, which is taken as a fixed value of 8.314 J / mol·K. -1 , T This is the real-time temperature value. e It is an exponential function. e >0, and e≠1; k(Cl) is a linear enhancement function, 0 < k(Cl) < 1.

[0023] Compared with the prior art, the upgrading method of the clean coal processing and upgrading system of the present invention has the following beneficial effects:

[0024] 1. This invention combines a single-stage ultrasonic reaction device and a two-stage ultrasonic reaction device with a multi-stage acid leaching process to treat high-chlorine coal, optimizing the leaching process, reducing unnecessary energy waste, and lowering production costs. By precisely controlling the leaching process, chlorides can be leached from solid high-chlorine coal quickly and effectively, with a high removal rate of water-soluble chloride ions, more thorough dechlorination, and improved production efficiency.

[0025] 2. This invention uses organic acids such as citric acid and ascorbic acid, and operates under mild conditions. It solves the environmental pollution problems caused by the use of high acid and high organic solvents in current dechlorination technologies, and is in line with the concept of green and environmentally friendly sustainable development.

[0026] 3. This invention removes chlorine from high-chlorine coal using ultrasonic technology. The cavitation effect of ultrasound generates strong shock waves and microjets that have a strong impact on the high-chlorine coal, accelerating the collision of high-chlorine coal particles, opening up the pore channels between coal particles, enabling effective contact between the solvent and the high-chlorine coal, and shortening the reaction time. In addition, ultrasound can clean the equipment after the reaction is completed. Attached Figure Description

[0027] Figure 1 This is a flowchart of the dechlorination method in an embodiment of the present invention;

[0028] Figure 2 This is a system flowchart of the dechlorination method in an embodiment of the present invention. Detailed Implementation

[0029] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention.

[0030] Based on the embodiments of this invention, all other embodiments obtained by those skilled in the art without inventive effort are within the scope of protection of this invention.

[0031] Furthermore, the technical solutions of the various embodiments of the present invention can be combined with each other, but only if they are feasible for those skilled in the art. If the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such combination of technical solutions does not exist and is not within the scope of protection claimed by the present invention.

[0032] See Figure 1and Figure 2 As shown, in order to achieve sufficient and efficient dechlorination of coal and ensure effective reduction of environmental pollution during subsequent coal combustion, this embodiment provides a method for upgrading a clean coal processing system. Specifically, the dechlorination processing equipment of this system mainly includes: a first-stage ultrasonic reactor, a second-stage ultrasonic reactor, a control system, and a monitoring system. The control system is used to precisely control the entire system's experimental process and equipment. The monitoring system mainly includes a monitoring module, a control module, and an adjustment module, used to regulate the first-stage and second-stage ultrasonic reactors to ensure the normal operation of the system. Based on the above equipment composition, the specific method for upgrading the clean coal processing system includes the following steps:

[0033] S1: First-stage acid leaching: Coal sample and organic acid are mixed at a liquid-to-solid ratio of 10 mL / g-15 mL / g to form a mixture of coal sample and organic acid; the mixture is then transported to a first-stage ultrasonic reactor for dechlorination reaction, with the ultrasonic reaction temperature set at 60℃-80℃, ultrasonic reaction power at 500W-1000W, and ultrasonic reaction time at 3min-20min; the ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time are controlled in real time during the reaction process, and the chlorine removal rate is detected in real time (the chlorine removal rate is explored through single-factor experiment principle), and the reaction parameters at the time when the chlorine removal rate is highest are determined as the optimal reaction parameters;

[0034] S2: Solid-liquid separation: After the acid leaching reaction time is completed, the coal sample and the organic acid mixture after the reaction are subjected to solid-liquid separation to obtain a first-stage acid leaching residue and a first-stage acid leaching solution, respectively.

[0035] S3: Second-stage acid leaching: The first-stage acid leaching residue is mixed with organic acid again at a liquid-solid ratio of 9mL / g-14mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The prepared mixture of the first-stage acid leaching residue and organic acid is placed in a second-stage ultrasonic reactor. The reaction parameters of the second-stage ultrasonic reactor are set to be the same as the optimal reaction parameters of the first-stage ultrasonic reactor in step S2, so as to achieve the dechlorination reaction of the mixture of the first-stage acid leaching residue and organic acid.

[0036] S4: Two-stage solid-liquid separation. After the two-stage acid leaching reaction time is completed, the mixture of the first-stage acid leaching residue and organic acid is subjected to solid-liquid separation to obtain the second-stage pickling solution and the second-stage pickling residue.

[0037] S5: Subsequent Processing: The second-stage acid leaching solution is returned to step S2 and injected into the first-stage ultrasonic reactor as an organic acid solvent to continue participating in the dechlorination reaction, achieving recycling. The second-stage acid leaching residue is washed with deionized water, collected, and dried to constant weight for subsequent analysis. After adding copper oxide precipitate to the first-stage acid leaching solution, solid-liquid separation is performed. The separated precipitate is evaporated and crystallized to obtain cuprous chloride crystals. The separated filtrate is returned to the second-stage acid leaching step as an organic acid solvent for recycling. Furthermore, the acid leaching residue separated from either the first or second-stage acid leaching can be used to prepare cuprous chloride crystals, facilitating the analysis of dechlorination effects at different stages and serving as a reference for setting ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time parameters.

[0038] Furthermore, the parameters for the dechlorination reaction process should be set according to the following requirements:

[0039] 1. Preparation of coal samples: The high-chlorine coal is crushed and screened to obtain high-chlorine coal samples that meet the particle size requirements for clean processing; the particle size of the crushed high-chlorine coal is generally 0.5mm-13mm.

[0040] 2. The organic acid used is citric acid, ascorbic acid, or a mixture of both in a certain proportion. Preferably, when using a mixture of citric acid and ascorbic acid, the mixing ratio is (1~2):(1~2). However, if necessary, the mixing ratio can be arbitrary and not specified. Furthermore, the concentration of the organic acid used in dechlorination should be controlled between 0.5 mol / L and 3 mol / L.

[0041] 3. The ultrasonic reaction temperature is 60℃-80℃, and the ultrasonic reaction time is 3min-20min.

[0042] 4. Both the first-stage and second-stage ultrasonic reaction devices are equipped with mechanical stirrers. For example, a motor is used to drive the rotating shaft, and a spiral stirring fan is installed on the rotating shaft to stir the mixture. In order to ensure the dechlorination efficiency and the dechlorination effect, the speed of the mechanical stirrer (i.e. the output speed of the motor) is designed to be 200r / min-300r / min.

[0043] 5. The ultrasonic frequencies of the first-stage and second-stage ultrasonic reactors are set between 20kHz and 40kHz, and the ultrasonic intensity is 1W / cm². 2 -5W / cm 2 Between these ranges, the ultrasonic response power is 500W-1000W.

[0044] Furthermore, in order to accurately control the parameter regulation during the reaction process, the control system consists of a central controller and ultrasonic power monitoring modules, real-time temperature monitoring modules, and chlorine element monitoring modules installed on the first and second ultrasonic reaction devices. The central controller is used to receive signals transmitted by the ultrasonic power monitoring modules, real-time temperature monitoring modules, and chlorine element monitoring modules. By monitoring the reaction parameters in real time during the reaction process, error correction is performed, and precise regulation of ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time is achieved during the reaction process.

[0045] Specifically, the control system's regulation of ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time can be determined according to the following formula:

[0046] ,

[0047] in, , , These are functions for the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module, respectively, used to convert the raw monitoring data into values ​​that are beneficial to the control signal. , , The weights of the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module are respectively ( ), for / / ,and ;

[0048] Its revised form is as follows:

[0049] ,

[0050] in, ,

[0051] Ae −E a / RT ,

[0052] =1+(1+k(Cl)),

[0053] In the formula, , , These are the adjustment factors for the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module over time, where 0 < <1, 0< <1, 0< <1; , , The weights of the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module are respectively. , for / / ,and ; a For power regulation slope, a >0; b The power control intercept represents the fundamental contribution at zero power. b ≥0; P This is the real-time power value; Ae −E a / RT For Arrhenius's formula, A Pre-exponential factor, A =10 9 ~10 13 s −1 , R This is the gas constant, which is taken as a fixed value of 8.314 J / mol·K. -1 , T This is the real-time temperature value. e It is an exponential function. e >0, and e ≠1; k(Cl) is a linear enhancement function, 0 < k(Cl) < 1.

[0054] In addition, this device employs a single-stage ultrasonic reaction device and a two-stage ultrasonic reaction device. Besides enabling precise control of reaction parameters, it also allows the ultrasonic waves to participate in cleaning the device after the reaction, resulting in a more thorough cleaning.

[0055] The following are the implementation steps for coal dechlorination reaction based on the optimal parameter conditions set according to the different crushing particle sizes of high-chlorine coal:

[0056] Implementation Method 1:

[0057] S1: Coal sample preparation: The high-chlorine coal was crushed and screened to separate coal samples with a particle size of 13mm.

[0058] S2: First-stage acid leaching: The coal sample and prepared organic acid are mixed at a liquid-to-solid ratio of 15 mL / g to obtain a mixture of coal sample and organic acid. The organic acid is a mixture of citric acid with a concentration of 3 mol / L and ascorbic acid with a concentration of 1.5 mol / L. In a first-stage ultrasonic reaction device, the mechanical stirrer speed is set to 300 r / min, the ultrasonic reaction temperature is 80℃, the ultrasonic reaction power is 1000W, and the ultrasonic reaction time is 20 min. When the temperature rises to the set value, the mixture is placed in a monitorable ultrasonic reaction device for dechlorination reaction. During the reaction process, the control system adjusts each reaction parameter and monitors the chlorine removal rate in real time to determine the optimal reaction parameters.

[0059] S3: Solid-liquid separation: After the acid leaching reaction time is completed, the coal sample and the organic acid mixture after the reaction are subjected to solid-liquid separation to obtain a first-stage acid leaching residue and a first-stage acid leaching solution.

[0060] S4: Two-stage acid leaching: The first-stage acid leaching residue and organic acid are slurried and mixed at a liquid-to-solid ratio of 14 mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The prepared mixture of the first-stage acid leaching residue and organic acid is placed in a two-stage ultrasonic reactor. The reaction parameters of the two-stage ultrasonic reactor are set to be the same as the optimal reaction parameters of the first-stage ultrasonic reactor to achieve the dechlorination reaction of the mixture of the first-stage acid leaching residue and organic acid.

[0061] S5: Two-stage solid-liquid separation. After the two-stage acid leaching reaction time is completed, the mixture of the first-stage acid leaching residue and organic acid is subjected to solid-liquid separation to obtain the second-stage pickling solution and the second-stage pickling residue.

[0062] S6: Subsequent processing: The second-stage acid leaching solution is returned to the first-stage acid leaching (S2 step) for further dechlorination. The second-stage acid leaching residue is washed three times with deionized water, collected, and dried to constant weight for subsequent analysis. Copper oxide is added to the separated first-stage acid leaching solution to precipitate it, followed by evaporation and crystallization to obtain cuprous chloride crystals. The filtered filtrate is returned to the second-stage acid leaching step as a solvent for organic acids and recycled.

[0063] Implementation Method Two:

[0064] S1: Coal sample preparation: The high-chlorine coal is crushed and screened to separate coal samples with a particle size of 6mm.

[0065] S2: First-stage acid leaching: The coal sample and prepared organic acid are mixed at a liquid-to-solid ratio of 12 mL / g to obtain a mixture of coal sample and organic acid. The organic acid is a mixture of citric acid with a concentration of 2 mol / L and ascorbic acid with a concentration of 1 mol / L. In a first-stage ultrasonic reaction device, the mechanical stirrer speed is set to 300 r / min, the ultrasonic reaction temperature is set to 60℃, the ultrasonic reaction power is set to 800W, and the ultrasonic reaction time is set to 15 min. When the temperature rises to the set value, the mixture is placed in a monitorable ultrasonic reaction device for dechlorination reaction. During the reaction process, the reaction parameters are adjusted by the control system, and the chlorine removal rate is monitored in real time to determine the optimal reaction parameters.

[0066] S3: Solid-liquid separation: After the acid leaching reaction time is completed, the coal sample and the organic acid mixture after the reaction are subjected to solid-liquid separation to obtain a first-stage acid leaching residue and a first-stage acid leaching solution.

[0067] S4: Two-stage acid leaching: The first-stage acid leaching residue and organic acid are slurried and mixed at a liquid-to-solid ratio of 11 mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The prepared mixture of the first-stage acid leaching residue and organic acid is placed in a two-stage ultrasonic reactor. The reaction parameters of the two-stage ultrasonic reactor are set to be the same as the optimal reaction parameters of the first-stage ultrasonic reactor to achieve the dechlorination reaction of the mixture of the first-stage acid leaching residue and organic acid.

[0068] S5: Two-stage solid-liquid separation. After the two-stage acid leaching reaction time is completed, the mixture of the first-stage acid leaching residue and organic acid is subjected to solid-liquid separation to obtain the second-stage pickling solution and the second-stage pickling residue.

[0069] S6: Subsequent processing: The second-stage acid leaching solution is returned to the first-stage acid leaching step for further dechlorination. The second-stage acid leaching residue is washed three times with deionized water, collected, and dried to constant weight for subsequent analysis. Copper oxide is added to the separated first-stage acid leaching solution to precipitate it, followed by evaporation and crystallization to obtain cuprous chloride crystals. The filtered filtrate is returned to the second-stage acid leaching step as a solvent for organic acids and recycled.

[0070] Implementation Method 3:

[0071] S1: Coal sample preparation: The high-chlorine coal is crushed and screened to separate coal samples with a particle size of 3mm.

[0072] S2: First-stage acid leaching: The coal sample and prepared organic acid are mixed at a liquid-to-solid ratio of 11 mL / g to obtain a mixture of coal sample and organic acid. The organic acid used is citric acid with a concentration of 1.5 mol / L and ascorbic acid with a concentration of 1 mol / L. In a first-stage ultrasonic reaction device, the mechanical stirring speed is set to 280 r / min, the ultrasonic reaction temperature is set to 60℃, the ultrasonic reaction power is set to 600 W, and the ultrasonic reaction time is set to 12 min. When the temperature rises to the set value, the mixture is placed in a monitorable ultrasonic reaction device for dechlorination reaction. During the reaction process, the reaction parameters are adjusted by the control system, and the chlorine removal rate is monitored in real time to determine the optimal reaction parameters.

[0073] S3: Solid-liquid separation: After the acid leaching reaction time is completed, the coal sample and the organic acid mixture after the reaction are subjected to solid-liquid separation to obtain a first-stage acid leaching residue and a first-stage acid leaching solution.

[0074] S4: Two-stage acid leaching: The first-stage acid leaching residue and organic acid are slurried and mixed at a liquid-to-solid ratio of 10 mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The prepared mixture of the first-stage acid leaching residue and organic acid is placed in a two-stage ultrasonic reactor. The reaction parameters of the two-stage ultrasonic reactor are set to be the same as the optimal reaction parameters of the first-stage ultrasonic reactor to achieve the dechlorination reaction of the mixture of the first-stage acid leaching residue and organic acid.

[0075] S5: Two-stage solid-liquid separation. After the two-stage acid leaching reaction time is completed, the mixture of the first-stage acid leaching residue and organic acid is subjected to solid-liquid separation to obtain the second-stage pickling solution and the second-stage pickling residue.

[0076] S6: Subsequent processing: The second-stage acid leaching solution is returned to the first-stage acid leaching step for further dechlorination. The second-stage acid leaching residue is washed three times with deionized water, collected, and dried to constant weight for subsequent analysis. Copper oxide is added to the separated first-stage acid leaching solution to precipitate it, followed by evaporation and crystallization to obtain cuprous chloride crystals. The filtered filtrate is returned to the second-stage acid leaching step as a solvent for organic acids and recycled.

[0077] Obviously, those skilled in the art can make various modifications and variations to this invention without departing from its spirit and scope. Therefore, if these modifications and variations fall within the scope of the claims of this invention and their equivalents, this invention also intends to include these modifications and variations.

Claims

1. A method for upgrading coal in a clean coal processing system, characterized in that, Includes the following steps: S1: First-stage acid leaching: Coal sample and organic acid are mixed at a liquid-to-solid ratio of 10mL / g-15mL / g to form a mixture of coal sample and organic acid; the mixture is then transported to a first-stage ultrasonic reactor for dechlorination reaction, with the ultrasonic reaction temperature set at 60℃-80℃, ultrasonic reaction power at 500W-1000W, and ultrasonic reaction time at 3min-20min; the ultrasonic reaction temperature, ultrasonic reaction power, and ultrasonic reaction time are adjusted in real time during the reaction process, and the chlorine removal rate is monitored in real time to determine the optimal reaction parameters for the period with the highest chlorine removal rate; S2: Perform solid-liquid separation on the mixture after the reaction to obtain a first-stage acid leaching residue and a first-stage acid leaching solution; S3: Second-stage acid leaching: The first-stage acid leaching residue and organic acid are slurried and mixed at a liquid-solid ratio of 9mL / g-14mL / g to form a mixture of the first-stage acid leaching residue and organic acid. The mixture is then placed in a second-stage ultrasonic reactor for dechlorination reaction, and the reaction parameters of the second-stage ultrasonic reactor are set to the optimal reaction parameters obtained in step S1. S4: Perform solid-liquid separation on the mixture after the reaction to obtain a second-stage acid leaching residue and a second-stage acid leaching solution; S5: Subsequent processing: The second-stage acid leaching solution is returned to step S1 as an organic acid solvent to continue participating in the dechlorination reaction in the first-stage ultrasonic reactor. The second-stage acid leaching residue is washed with deionized water, collected, and dried to constant weight for subsequent analysis. After adding copper oxide to the first-stage acid leaching solution to precipitate, solid-liquid separation is performed. The separated precipitate is evaporated and crystallized to obtain cuprous chloride crystals. The separated filtrate is returned to step S3 as an organic acid solvent for recycling. The control of ultrasonic response temperature, ultrasonic response power, and ultrasonic response time is determined according to the following formula: ， in, , Ae −E a / RT ， =1+(1+k(Cl)), In the formula, , , These are the adjustment factors for the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module over time, where 0 < <1, 0< <1, 0< <1; , , The weights of the ultrasonic power monitoring module, the real-time temperature monitoring module, and the chlorine element monitoring module are respectively. , for / / ,and ; a For power regulation slope, a >0; b The power control intercept represents the fundamental contribution at zero power. b ≥0; P This is the real-time power value; Ae −E a / RT For Arrhenius's formula, A Pre-exponential factor, A =10 9 ~10 13 s −1 , R This is the gas constant, which is taken as a fixed value of 8.314 J / mol·K. -1 , T This is the real-time temperature value. e It is an exponential function. e >0, and e ≠1; k(Cl) is a linear enhancement function, 0 < k(Cl) < 1.

2. The method for upgrading a clean coal processing system according to claim 1, characterized in that, The coal sample that participated in the dechlorination reaction had a particle size of 0.5 mm to 13 mm.

3. The upgrading method of a clean coal processing and upgrading system according to claim 1, characterized in that, The organic acid is citric acid, ascorbic acid, or a mixture of citric acid and ascorbic acid, wherein the mixing ratio of citric acid and ascorbic acid is (1~2):(1~2).

4. The method for upgrading a clean coal processing system according to claim 3, characterized in that, The concentration of the organic acid is 0.5 mol / L to 3 mol / L.

5. The method for upgrading a clean coal processing system according to claim 1, characterized in that, The mechanical stirrers in the first-stage and second-stage ultrasonic reaction devices rotate at a speed of 200 r / min to 300 r / min.

6. The upgrading method of a clean coal processing and upgrading system according to claim 1, characterized in that, The ultrasonic frequency of the first-stage and second-stage ultrasonic reactors is set to 20kHz-40kHz, and the ultrasonic intensity is 1W / cm². 2 -5W / cm 2 .

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