CN111977993B - Device and method for performing desulfurization or ash melting on returned stone and returned sand pulping in soda production - Google Patents
Device and method for performing desulfurization or ash melting on returned stone and returned sand pulping in soda production Download PDFInfo
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- CN111977993B CN111977993B CN201910422205.1A CN201910422205A CN111977993B CN 111977993 B CN111977993 B CN 111977993B CN 201910422205 A CN201910422205 A CN 201910422205A CN 111977993 B CN111977993 B CN 111977993B
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B2/00—Lime, magnesia or dolomite
- C04B2/02—Lime
- C04B2/04—Slaking
- C04B2/08—Devices therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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Abstract
The invention relates to a device and a method for carrying out desulfurization or ash melting on slurry prepared from returned stones and returned sands in the production of soda, wherein the method comprises the steps of carrying out wet grinding on small-particle returned stones and returned sands to obtain slurry, then shunting the slurry out of an emulsion and solid fine sands through a spiral sand washer, sending the emulsion into a power plant for desulfurization, and sending the solid fine sands into an ash melting machine for ash melting after pulverization; and the ground slurry can be directly sent to an ash melting process, so that the ash melting concentration is greatly improved, and the consumption of raw materials in the production of the soda ash is reduced. The implementation of the returned sand pulping combined production process reduces the production cost of soda production enterprises and thermoelectric companies, adapts to the current environment-friendly situation and the requirement of enterprise development, and provides favorable guarantee for enterprises to walk sustainable development roads.
Description
Technical Field
The invention relates to comprehensive utilization of solid wastes generated in the industry of soda plant production by ammonia-soda process, in particular to a device and a method for desulfurizing or ashing returned stone and returned sand pulping in soda production.
Background
Soda ash is the basic industrial raw material with the largest yield and wide application in the basic chemical industry. At present, China is a world-wide soda production country and is the only world-wide soda production country with three mature production processes of soda ash, ammonia soda and natural soda. In soda ash production enterprises in China, the production process for preparing soda ash by an ammonia-soda process is mainly used. However, in the prior art, when soda ash is produced by an ammonia-soda process, three solid wastes are inevitably generated in the limestone calcining process: return sand, return stone and crushed stone. With the increase of environmental protection, the three solid wastes generated in the limestone calcining process severely restrict the sustainable development of enterprises and are also the bottleneck restricting the development of enterprises at present.
In the patent "method for producing desulfurizer from solid waste produced in soda plant industry" (patent application number: 201310121724.7), return stone, return sand and broken stone are uniformly mixed, and then are ground by ball mill and powder-selected, and then are fed into finished product bin. The process converts the solid three wastes into the high-quality limestone powder desulfurizer, but the process has serious defects which are mainly shown as follows: firstly, the yield of the returned stones, the returned sands and the crushed stones generated every day reaches about 1000 tons by taking an enterprise producing 120 ten thousand tons of soda ash every year as a calculation, and the processing capacity of the 1000 tons of grinding and desulfurizing processing every day is difficult to achieve; secondly, due to the physicochemical properties of returned stone and returned sand, the materials have the phenomenon of pulverization, thereby causing serious pollution to the environmental sanitation of the production site; thirdly, the waste generated after the grinding and the desulphurization cannot meet the requirements of zero pollution and zero emission; fourthly, due to the physicochemical properties of returned stone and returned sand, the material has the pulverization phenomenon, and the conveying pipeline and the equipment are seriously blocked in the desulfurization process of the power plant, so that the equipment cannot normally run.
Disclosure of Invention
Aiming at the problems, the invention provides a method for preparing a lime-fly ash by wet grinding return stone and return sand with the granularity of less than 40mm, which are generated in the limestone calcining process, and then shunting emulsion and solid fine sand through a spiral sand washer, wherein the emulsion is sent into a power plant for desulfurization, and the solid fine sand is pulverized and then sent into an ash melting machine for ash melting; the invention can directly send the ground slurry into the ash melting process, thereby not only avoiding the serious influence on the environment caused by the non-removal of returned sand due to the shutdown of a power plant, but also greatly improving the ash melting concentration and reducing the raw material consumption in the production of the calcined soda. The implementation of the returned sand pulping combined production process reduces the production cost of soda production enterprises and thermoelectric companies, provides favorable measures for soda in treating solid waste sand, is suitable for the current environment-friendly situation and the requirement of enterprise development, and provides favorable guarantee for enterprises to walk sustainable development roads.
The device comprises a return sand bin for storing return stones and return sands, a material outlet of the return sand bin is connected with a material inlet of a ball mill through a feeding pipe, a slurry outlet of the ball mill is connected with a buffer barrel for temporarily storing slurry through a pipeline, a slurry output pipeline of the buffer barrel is divided into a first branch pipe and a second branch pipe, the first branch pipe is connected with a material inlet of a spiral sand washer through a first slurry pump, a solid fine sand outlet of the spiral sand washer is connected with an ash melting machine through a material conveying device, an emulsion outlet of the spiral sand washer is connected with a desulfurization device of a power plant through a conveying pipeline, and the second branch pipe is connected with the ash melting machine through a second slurry pump.
Further, the first branch pipe is branched out of a third branch pipe after the first slurry pump and connected to the liquid feeding hole of the sand return bin, and/or the second branch pipe is branched out of a fourth branch pipe after the second slurry pump and connected to the liquid feeding hole of the sand return bin.
Furthermore, a washing water inlet of the buffer barrel is connected with a washing water input pipeline, a washing water pump for pressurizing is arranged on the washing water input pipeline, and a valve for controlling the washing water to enter the buffer barrel is arranged on the washing water input pipeline between the washing water pump and the buffer barrel.
Furthermore, a first pneumatic adjusting valve is arranged on the first branch pipe.
Furthermore, the washing water pump and a branch pipe which is branched from a washing water input pipeline between the valves for controlling the washing water to enter the buffer barrel are connected with a washing water inlet of the sand return bin after passing through a second pneumatic regulating valve.
The returned stone and the returned sand in the application refer to that limestone in the production of soda ash is calcined to generate lime and then reacts with water (called lime melting in the industry) to generate calcium hydroxide emulsion (called lime melting in the industry), some limestone is not completely calcined and is melted in the form of limestone, the large-particle stone is called the returned stone after the lime melting process, and the small-particle stone (like sand passing) is called the returned sand.
The invention further relates to a method for pulping return stone and return sand and desulfurizing or incinerating the return stone and the return sand, which comprises the following steps:
(1) sieving the returned stone and the returned sand (for example, sieving by using a returned stone rotary sieve), feeding the large-sized returned stone (with the granularity of more than 40mm) into a lime kiln for secondary calcination, feeding a mixture of small-particle returned stone (with the granularity of 10-40mm) and the returned sand (with the granularity of generally less than 10 mm) into a returned sand bin,
(2) in the step (1), the mixed material of the return stone and the return sand in the return sand bin is driven by washing water (the flow of the mixed material entering the ball mill can be 7-11t/h (calculated by 60 ten thousand tons of soda enterprises produced in the year), and the flow of the washing water can be 20-25m3H) feeding the slurry into a ball mill through a feeding pipe, grinding the slurry by the ball mill (generally reaching the particle size range of 12-286 mu m) to obtain slurry (the solid-liquid ratio of the slurry is 15-23%, and the CaO concentration of the slurry is kept at 15-35 tt), conveying the slurry to a buffer barrel,
(3) pumping the slurry in the buffer barrel in the step (2) to a spiral sand washer, separating emulsion from solid fine sand in the slurry by the spiral sand washer, feeding the emulsion slurry to a power plant for desulfurization, and feeding the solid fine sand to an ash melting machine procedure of the power plant for ash melting; and/or
And (3) directly pumping the slurry in the buffer barrel in the step (2) to an ash melting machine for secondary ash melting.
Under the condition that the power plant does not need or the required amount is less than the yield of the method, the slurry in the buffer barrel in the step (2) is directly pumped to an ash melting machine for secondary ash melting, or part of the desulfurized ash is melted and part of the desulfurized ash is directly melted, and under the condition that the desulfurized ash and the directly melted ash are simultaneously carried out, the proportion of the desulfurized ash and the directly melted ash can be set according to the requirement.
The process can adopt a phi 1830 x 7000 double-bin wet ball mill with the highest rotation speed of 24.3r/min, the production capacity of 7.8-13.8t/h and the effective volume of 16m3. This equipment adopts frequency conversion operation with high-voltage motor, and the regulation of accessible frequency changes the rotational speed of equipment, avoids the material to reduce the back, reduces the impact of ball mill built-in steel ball to the equipment barrel, improve equipment life.
Considering that solid fine sand particles in the slurry are smaller, a spiral sand washer with the spiral diameter of 500mm, the processing capacity (calculated according to the solid fine sand amount) of 4-9t/h and the spiral rotating speed of 8-12.5r/min can be adopted.
If the separated emulsion is used excessively or is stopped after being sent into a power plant, the slurry ground by the ball mill can be directly sent to an ash melting machine for secondary ash melting through a buffer barrel, so that the serious influence on the environment caused by no sand return due to the stop of the power plant is avoided. The ash melting temperature in the ash melting process can be effectively increased by 2-5 ℃, the concentration of the lime milk is increased by 3-5tt, and 50kg of limestone can be saved per ton of soda ash.
Further, the slurry in the buffer barrel (usually accounting for 30-50 wt% of the total slurry of the ball mill) is conveyed to a sand return bin, and the slurry enters the ball mill for secondary grinding. Damage to the lining plate of the ball mill caused by the fact that the feeding amount of the ball mill is reduced (for example, the feeding amount is lower than the conventional feeding amount) can be effectively avoided.
Further, in the step (2), when the solid-to-liquid ratio of the slurry entering the buffer barrel is too high (for example, the solid-to-liquid ratio in the slurry is greater than 23%), the washing water is conveyed to the buffer barrel through the washing water input pipeline for diluting the solid-to-liquid ratio of the slurry (until the solid-to-liquid ratio is reduced to 15-23%), and the pipeline is prevented from being blocked due to conveying.
In the step (2), washing water is sent into the sand return bin, the washing water drives the mixed material to enter the inside of the ball mill through a feeding pipe (a preferable flow pipe), the blocking of the sand return bin caused by the pulverization of the returned sand due to the long-time shutdown of the ball mill is avoided, and the field production environment can be effectively improved by feeding through the feeding flow pipe.
And (2) washing water is connected to the upper part of the buffering barrel and used for washing the whole slurry conveying pipeline by adopting the washing water when the ball mill stops running, and the washing water is concentrated and precipitated and then flows to a production water system of a whole plant, so that the pipeline is prevented from being blocked due to the fact that the pipeline stops for a long time and the slurry in the pipeline is pulverized.
The invention has the beneficial effects that:
(1) the process of the invention can effectively treat the returned sand in the production of the sodium carbonate and the environmental pollution caused by pulverization.
(2) By implementing the process, the desulfurization efficiency of the power plant can reach more than 99 percent, the production cost of the power plant is reduced, and meanwhile, the zero emission of an enterprise is guaranteed.
(3) The slurry in the process of the invention directly enters an ash melting machine, the ash melting temperature in the ash melting process can be effectively increased by 2-5 ℃, the concentration of lime milk is increased by 3-5tt, and 50kg of limestone can be saved per ton of soda ash. And the problem of serious environmental pollution caused by sand return accumulation due to outage of a power plant can also be solved.
(4) The process disclosed by the invention is combined with a new process for co-production of saline-alkali calcium, so that measures for realizing zero emission and zero pollution of return sand are created for the first time in the soda industry, and a postshield is provided for sustainable development of enterprises.
Drawings
FIG. 1 is a schematic diagram of an apparatus for desulfurizing or incinerating returned stone and returned sand in pulping in soda production.
Reference numerals:
a sand return bin 1, a ball mill 2, a feeding flow pipe 3, a buffer barrel 4, a first slurry pump 5, a second slurry pump 6, a first pneumatic regulating valve 7, a second pneumatic regulating valve 8, a valve 9 and a spiral sand washer 10,
the slurry outlet pipeline L, the first branch pipe L1, the second branch pipe L2, the third branch pipe L3, the fourth branch pipe L4, the washing water inlet pipeline L5 and the fifth branch pipe L6.
Detailed Description
The invention is further illustrated by the following figures and examples.
As shown in figure 1, the device for performing desulfurization or ash removal on slurry of returned stone and returned sand in the production of soda ash comprises a returned sand bin 1 for storing the returned stone and the returned sand, a material outlet of the returned sand bin 1 is connected with a material inlet of a ball mill 2 through a feeding flow pipe 3, a slurry outlet of the ball mill 2 is connected with a buffer barrel 4 for temporarily storing slurry through a pipeline, a slurry output pipeline L of the buffer barrel 4 is divided into a first branch pipe and a second branch pipe (L1 and L2), the first branch pipe L1 is connected with a material inlet of a spiral sand washer 10 through a first slurry pump 5, a solid fine sand outlet of the spiral sand washer 10 is connected with an ash remover through a material conveying device, an emulsion outlet of the spiral sand washer 10 is connected with a desulfurization device of a power plant through a slurry conveying pipeline, the first branch pipe L1 is divided into a third branch pipe L3 through the first slurry pump 5, and the second branch pipe L2 is connected with the ash remover through a second slurry pump 6, the second branch pipe L2 is branched into a fourth branch pipe L4 after passing through the second slurry pump 6, and the third branch pipe L3 is connected with the liquid feeding hole of the sand return bin 1 after being converged with the fourth branch pipe L4.
A washing water inlet of the buffer barrel 4 is connected with a washing water input pipeline L5, a washing water pump (not shown) for pressurizing is arranged on the washing water input pipeline, and a valve 9 for controlling the washing water to enter the buffer barrel is arranged on the washing water input pipeline between the washing water pump and the buffer barrel.
The first branch pipe L1 is provided with a first pneumatic adjustment valve 7.
A fifth branch pipe L6 branched from the washing water input pipeline between the washing water pump and the valve 9 passes through the second pneumatic regulating valve 8 and then is connected with the washing water inlet of the sand return bin 1.
Example 1
A method for carrying out desulfurization or ash removal on return stone and return sand pulping in soda production comprises the following steps:
(1) sieving the returned stone and the returned sand at a speed of 12-16t/h (calculated by enterprises producing 60 million tons of soda annually) by using a returned stone rotary sieve, feeding the large returned stone with the granularity of more than 40mm into a lime kiln for secondary calcination, sieving a mixture of small-particle returned stone and returned sand with the granularity of less than 40mm at a speed of 7-11t/h (calculated by enterprises producing 60 million tons of soda annually) into a sand return bin,
(2) close offThe valve on the washing water input pipeline is opened, the second pneumatic regulating valve is opened, and the washing water is 20-25m3Inputting the flow rate of per hour into a sand return bin, driving the mixed material of the return stones and the return sands in the sand return bin in the step (1) to enter a ball mill through a feeding flow pipe under the driving of washing water at the speed of 7-11t/h (calculated by 60 ten thousand tons of soda enterprises produced every year), grinding the mixed material to the granularity of 12-286 mu m through the ball mill to obtain slurry with the solid-to-liquid ratio of 15-23% and the CaO concentration of 15-35 tt, and conveying the slurry to a buffer barrel,
(3) the slurry in the buffer barrel in the step (2) is pressurized by a first slurry pump and then is conveyed to a spiral sand washer through a first branch pipe, emulsion and solid fine sand are separated out by the spiral sand washer, the emulsion is conveyed to a power plant for desulfurization, and the content of sulfur dioxide in the flue gas of the power plant can be reduced to 8mg/m3The following (national standard 100 mg/m)3And (b) feeding the solid fine sand into an ash melting machine for melting ash.
When the feeding amount of the ball mill is reduced (for example, the feeding amount is lower than the conventional feeding amount), the slurry in the buffer barrel is partially conveyed to the sand return bin, and the slurry enters the ball mill for grinding for the second time. The ball mill is used for accessing washing water above the buffering barrel when the ball mill stops running, and washing water is adopted to wash the pipeline so as to avoid pipeline blockage caused by slurry pulverization in the pipeline due to long-time stopping of the pipeline.
Example 2
A method for lime slaking of returned stone and returned sand pulping in soda production comprises the following steps:
(1) sieving the returned stone and the returned sand at a speed of 12-16t/h (calculated by enterprises producing 60 million tons of soda annually) by using a returned stone rotary sieve, feeding the large returned stone with the granularity of more than 40mm into a lime kiln for secondary calcination, sieving a mixture of small-particle returned stone and returned sand with the granularity of less than 40mm at a speed of 7-11t/h (calculated by enterprises producing 60 million tons of soda annually) into a sand return bin,
(2) closing the valve on the washing water input pipeline, opening the second pneumatic regulating valve, and controlling the washing water to be 20-25m3Inputting the flow of/h into a sand return bin, driving the mixed material of the return stone and the return sand in the sand return bin in the step (1) to enter a ball mill through a feeding flow pipe under the driving of washing water at the speed of 7-11t/h (calculated by enterprises producing 60 ten thousand tons of soda annually), and grinding the mixed material to the particle size range of 12-286 mu m by the ball mill to obtain solidConveying the slurry with the liquid ratio of 15-23% and the CaO concentration of 15-35 tt to a buffer barrel,
(3) and (3) the slurry in the buffer barrel in the step (2) is pressurized by the second slurry pump and then is conveyed to the ash melting machine for secondary ash melting, so that the phenomenon that returned sand is not removed due to the outage of a power plant and the environment is seriously influenced is avoided. The ash melting temperature can be effectively increased by 2-5 ℃, the lime milk concentration is increased by 3-5tt, and 50Kg of limestone can be saved per ton of soda ash.
Example 3
A method for carrying out desulfurization or ash removal on return stone and return sand pulping in soda production comprises the following steps:
(1) sieving the returned stone and the returned sand at a speed of 12-16t/h (calculated by enterprises producing 60 million tons of soda annually) by using a returned stone rotary sieve, feeding the large returned stone with the granularity of more than 40mm into a lime kiln for secondary calcination, sieving a mixture of small-particle returned stone and returned sand with the granularity of less than 40mm at a speed of 7-11t/h (calculated by enterprises producing 60 million tons of soda annually) into a sand return bin,
(2) closing the valve on the washing water input pipeline, opening the second pneumatic regulating valve, and controlling the washing water to be 20-25m3Inputting the flow rate of per hour into a sand return bin, driving the mixed material of the return stones and the return sands in the sand return bin in the step (1) to enter a ball mill through a feeding flow pipe under the driving of washing water at the speed of 7-11t/h (calculated by 60 ten thousand tons of soda enterprises produced every year), grinding the mixed material to the granularity of 12-286 mu m through the ball mill to obtain slurry with the solid-to-liquid ratio of 15-23% and the CaO concentration of 15-35 tt, and conveying the slurry to a buffer barrel,
(3) after being pressurized by the first slurry pump, the slurry part in the buffer barrel in the step (2) is conveyed to a spiral sand washer through a first branch pipe, emulsion and solid fine sand are separated out by the spiral sand washer, the emulsion is conveyed to a power plant for desulfurization, and the content of sulfur dioxide in the flue gas of the power plant can be reduced to 8mg/m3The following (national standard 100 mg/m)3Within), sending the solid fine sand into an ash melting machine for melting ash,
(4) and (3) the residual part of the slurry in the buffer barrel in the step (2) is pressurized by the second slurry pump and then is conveyed to the ash melting machine for secondary ash melting, so that the condition that the capacity of the ball mill is excessive due to the reduction of the desulfurization amount of the power plant can be avoided. The improvement of ash melting temperature and ash emulsion concentration is helpful to a certain extent, and the consumption of soda production is reduced.
Example 4
(1) Sieving the returned stone and the returned sand at a speed of 16-20t/h (calculated by enterprises producing 60 million tons of soda annually and under the condition of lime calcination) by using a returned stone rotary sieve, feeding the large returned stone with the granularity of more than 40mm into a lime kiln for secondary calcination, sieving a mixture of small-particle returned stone and returned sand with the granularity of less than 40mm at a speed of 10-13t/h (calculated by enterprises producing 60 million tons of soda annually) into a sand return bin,
(2) closing the valve on the washing water input pipeline, opening the second pneumatic regulating valve, and controlling the washing water to be 20-25m3Inputting the flow of/h into a sand return bin, feeding the mixed material of the return stone and the return sand in the sand return bin in the step (1) into a ball mill through a feeding flow pipe at the speed of 10-13t/h (calculated by 60 ten thousand tons of soda enterprises produced every year) under the driving of washing water, grinding the mixed material by the ball mill (to the granularity range of 12-286 mu m) to obtain slurry with the solid-to-liquid ratio of more than 23 percent and the CaO concentration of 15-35 tt, conveying the slurry into a buffer barrel through a washing water input pipeline, conveying the washing water into the buffer barrel through a washing water input pipeline for diluting the slurry to reduce the solid-to-liquid ratio to 15-23 percent,
(3) and (3) after the slurry in the buffer barrel in the step (2) is pressurized by the first slurry pump, the slurry is conveyed to a spiral sand washer through a first branch pipe, emulsion and solid fine sand are separated out by the spiral sand washer, the emulsion is conveyed to a power plant for desulfurization, and the solid fine sand is conveyed to an ash melting machine for ash melting.
Claims (10)
1. A device for desulfurizing or ashing returned stones and returned sand in pulping in soda production is characterized by comprising a returned sand bin for storing the returned stones and the returned sand, wherein a material outlet of the returned sand bin is connected with a material inlet of a ball mill through a feeding pipe;
the first branch pipe is connected with the liquid feeding hole of the sand return bin after being branched out by the third branch pipe after the first slurry pump, and/or the second branch pipe is connected with the liquid feeding hole of the sand return bin after being branched out by the fourth branch pipe after the second slurry pump.
2. The apparatus of claim 1, wherein the first branch line is provided with a first pneumatic regulator valve.
3. The device according to claim 1 or 2, wherein the washing water inlet of the buffer barrel is connected with a washing water input pipeline, a washing water pump for pressurizing is arranged on the washing water input pipeline, and a valve for controlling the washing water to enter the buffer barrel is arranged on the washing water input pipeline between the washing water pump and the buffer barrel.
4. The apparatus of claim 3, wherein a branch pipe branched from the washing water input pipe between the washing water pump and the valve for controlling the washing water to enter the buffer barrel is connected with the washing water inlet of the sand return bin after passing through the second pneumatic control valve.
5. A method of slurrying and desulfurizing or ashing return rock, return sand, the method comprising:
(1) after the return stones and the return sands are screened, the large return stones are sent into a lime kiln for secondary calcination, the mixture of the small return stones and the return sands is sent into a return sand bin,
(2) in the step (1), the mixed material of the return stone and the return sand in the return sand bin enters the ball mill through the feeding pipe under the driving of washing water, slurry obtained after grinding by the ball mill is conveyed to the buffer barrel,
(3) pumping the slurry in the buffer barrel in the step (2) to a spiral sand washer, separating emulsion and solid fine sand by the spiral sand washer, feeding the emulsion to a power plant for desulfurization, and feeding the solid fine sand to an ash melting machine for ash melting; and/or
And (3) directly pumping the slurry in the buffer barrel in the step (2) to an ash melting machine for secondary ash melting.
6. The method of claim 5, wherein the particle size of the large return stone is greater than 40mm and the particle size of the small return stone is 10-40 mm.
7. The method as claimed in claim 6, wherein when the feeding amount of the ball mill is reduced, the slurry in the buffer barrel is partially conveyed to the sand return bin, and the slurry enters the ball mill for grinding twice.
8. The method according to claim 6, wherein in the step (2), when the concentration of the slurry entering the buffer barrel is too high, the washing water is conveyed to the buffer barrel through the washing water input pipeline for diluting the slurry, so that the blockage of the pipeline caused by the conveying is avoided.
9. The method as claimed in claim 8, wherein when the solid-to-liquid ratio of the slurry entering the buffer tank is more than 23%, the washing water is delivered to the buffer tank through the washing water input pipeline for diluting the slurry to the solid-to-liquid ratio of 15-23%.
10. The method according to claim 6, wherein in the step (2), washing water is introduced above the buffering barrel for flushing the pipeline with the washing water when the ball mill stops operating.
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