CN113562809A - Comprehensive recycling process for gasified fine slag - Google Patents
Comprehensive recycling process for gasified fine slag Download PDFInfo
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- 239000002893 slag Substances 0.000 title claims abstract description 47
- 238000004064 recycling Methods 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 32
- 230000008569 process Effects 0.000 title claims abstract description 24
- 239000003245 coal Substances 0.000 claims abstract description 92
- 239000010866 blackwater Substances 0.000 claims abstract description 38
- 239000000706 filtrate Substances 0.000 claims abstract description 32
- 238000003756 stirring Methods 0.000 claims abstract description 26
- 239000003250 coal slurry Substances 0.000 claims abstract description 16
- 238000002485 combustion reaction Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 239000002131 composite material Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 53
- 238000011010 flushing procedure Methods 0.000 claims description 20
- 239000012065 filter cake Substances 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 9
- 238000012423 maintenance Methods 0.000 claims description 5
- 235000011837 pasties Nutrition 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 238000002309 gasification Methods 0.000 abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 21
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 238000011160 research Methods 0.000 description 6
- 238000004062 sedimentation Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 2
- 239000003830 anthracite Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011835 investigation Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002352 surface water Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000010884 boiler slag Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000007405 data analysis Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000009795 derivation Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003631 expected effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
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Abstract
The invention discloses a comprehensive recycling process of gasified fine slag, which comprises the following steps: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank to a centrifuge through a settling tank underflow pump for solid-liquid separation, conveying the black water out of the centrifuge into a wet ash conveying system, enabling the black water to fall into a stirring bin for stirring treatment, controlling an outlet to a screw feeder through a hydraulic gate valve, finally, conveying the black water to a composite coal slime pipeline after pressurization through a wet ash conveying pump, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge into a filtrate tank, and conveying the filtrate in the filtrate tank back to the settling tank through a pipeline through the filtrate pump. The invention solves the problems of low utilization rate, high recovery cost and environmental pollution of the existing gasification fine slag. The invention adopts the combination of the horizontal screw centrifuge and the coal slurry pump, and the dense phase region of the boiler feeds materials, thereby realizing the high-efficiency and clean comprehensive recycling of gasified fine slag and simultaneously realizing the low-nitrogen combustion of the boiler.
Description
Technical Field
The invention belongs to the field of waste recycling, and particularly relates to a comprehensive recycling process of gasified fine slag.
Background
Comprehensive utilization of fine slag belongs to the derivation problem brought by the development of entrained flow bed gasification technology in the field of modern coal chemical industry. Taking Hua Yi company as an example, the whole year aerospace furnaces produce over 7 million tons (dry basis) of fine slag. How to utilize the fine slag comprehensively and efficiently is a general concern problem in the industry, most space furnace devices are treated in a stacking and selling (extremely low price) mode at present, and the purpose of utilizing the residual carbon in the fine slag is basically not achieved by recycling a small amount of fine slag comprehensively.
The traditional fine slag treatment of the space furnace adopts a vacuum belt filtering system to dehydrate the slime water settled in the settling tank of the space furnace, and the water content and the carbon residue of the slime dehydrated by the vacuum belt filtering system are both 30-50% (directly related to the coal quality). Because the coal slime contains a certain heat value (about 3000 Kcal), some companies can sell 10-50 yuan per ton in coal-shortage areas by adopting an external selling mode, but cannot sell the coal slime in coal-rich areas basically, and are basically in an embarrassing situation where money needs to be drawn and people can handle the coal slime.
And coal slime treated by a belt filter enters a coal slime recycling system by some companies, and is pumped into a boiler for mixed combustion. Researches show that due to the vacuum filtering system adopted by the belt filter, the treated coal slime has very dry surface, does not contain surface water basically and is difficult to stir, but the water content in pores of the coal slime is higher, so that water is added into a stirring bin for stirring before entering a coal slime recycling system, and the coal slime enters a strange circle for dehydration and water addition, thereby causing serious energy waste. Meanwhile, the coal slime enters the boiler and is sprayed from the top, so that the heat value of the coal slime is basically not utilized. According to company demonstration, the method only passes the fine slag of the space furnace through secondary fire, solves the problem of transporting wet coal slime, does not utilize the heat value of the fine slag, and has the most direct expression that the coal consumption of boiler steam is not reduced after the coal slime is mixed and burnt.
In recent two years, plate frame desliming projects are applied to some companies, and a plate frame filter pressing system has higher dehydration efficiency, so that the water content of the dehydrated coal slime can be controlled to be about 20%, and then the coal slime and fuel coal are directly mixed and then fed into a boiler for blending combustion, thereby solving the problem of utilization of fine slag. However, the company researches and finds that the treatment mode brings two new problems: firstly, the operation cost of plate-and-frame filter pressing is higher and is more than twice of the operation cost of a belt filter; secondly, the coal slime still falls to the ground after dehydration, and basically is mixed by a forklift or a belt, so that a series of new problems of secondary dust pollution, fuel coal quality fluctuation and the like are caused.
Disclosure of Invention
In order to overcome the defects of low utilization rate, high recovery cost and environmental pollution of the conventional gasification fine slag, the invention provides a comprehensive gasification fine slag recycling process which adopts a horizontal screw centrifuge and a coal slime pump to combine and feeds materials in a dense phase region of a boiler, realizes high-efficiency and clean comprehensive recycling of the gasification fine slag and realizes low-nitrogen combustion of the boiler.
The technical scheme adopted by the invention for realizing the purpose is as follows:
a comprehensive recycling process of gasified fine slag comprises the following steps: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank to a centrifuge through a settling tank underflow pump for solid-liquid separation, conveying the black water out of the centrifuge into a wet ash conveying system, enabling the black water to fall into a stirring bin for stirring treatment, controlling an outlet to a screw feeder through a hydraulic gate valve, finally, conveying the black water to a composite coal slime pipeline after pressurization through a wet ash conveying pump, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge into a filtrate tank, and conveying the filtrate in the filtrate tank back to the settling tank through a pipeline through the filtrate pump.
Further, 15-25 wt% of high-solid-content black water is sent to a centrifugal machine for solid-liquid separation, the coal slime contains 35-45 wt% of water, the coal slime is sent out of the centrifugal machine and enters a wet ash conveying system, the wet ash conveying system falls into a stirring bin for stirring treatment, and the pasty coal slime with the water content of 40-60% and the pumpability contains water.
Furthermore, a pipeline distributor is further arranged between the wet ash conveying pump and the boiler, and the pipeline distributor is further connected with an intermediate slag field.
Preferably, the boiler is fed with coal slurry at a location 800mm above the point of entry of the fuel coal.
Furthermore, a flushing water system is connected to the centrifugal machine, one path of the flushing water system is connected with the centrifugal machine, and the other path of the flushing water system is connected with the boiler through a flushing water pump.
Furthermore, the bottom flow pump of the settling tank is also connected with a filter through a pipeline, and the filter can be pumped to the filter from the bottom flow pump of the settling tank for filtering under the condition of maintenance of the centrifuge, wherein the water content of a filter cake is 45-55 wt%, and the filter cake is directly loaded after being taken out of the filter.
Preferably, the centrifuge is a horizontal screw centrifuge.
The invention mainly aims at the current situation of fine slag recycling in the current industry to fully investigate, analyze and demonstrate problems encountered in the recycling process, creatively adopts a centrifuge and coal slime recycling device to form, solves various problems existing in the centrifuge and the coal slime recycling device, and greatly enhances the operation stability of the whole recycling system. Meanwhile, the mode of feeding the coal slime into the boiler is fully demonstrated, the related parts are specially modified, the combustion state of the fine slag in the boiler is comprehensively improved, the coal consumption of the boiler is greatly reduced, and the heat value of the fine slag is fully utilized.
The mode mainly overturns the traditional fine slag treatment mode of the space furnace, optimizes and combines the fine slag treatment mode again by using relatively mature processes in the chemical industry on the basis of fully demonstrating the current situation of comprehensive utilization of the fine slag in the investigation and research industry, and solves the problem of connection and matching among different process routes. Meanwhile, the condition that the coal slime heat value utilization rate is not high is discussed and demonstrated, the coal consumption of a boiler is greatly reduced by changing the way of recycling the coal slime, and the heat value utilization of fine slag is maximized; the fine slag of the space furnace is completely eaten and squeezed, and a whole set of green, efficient and environment-friendly optimization scheme is provided for comprehensive utilization of the fine slag of the space furnace and even comprehensive utilization of the fine slag of the entrained-flow bed gasification furnace.
Drawings
The invention is further described with reference to the accompanying drawings, in which:
FIG. 1 is a process flow diagram of the present invention;
description of reference numerals: 1. the system comprises a settling tank, 2, a settling tank underflow pump, 3, a centrifugal machine, 4, a stirring bin, 5, a screw feeder, 6, a wet ash conveying pump, 7, a pipeline distributor, 8, a washing water pump, 9, a filtrate tank, 10 and a filtrate pump.
Detailed Description
Example 1
The comprehensive recycling process of the gasified fine slag comprises the following steps: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank 1 to a centrifuge 3 through a settling tank underflow pump 2 for solid-liquid separation, discharging the black water out of the centrifuge 3 into a wet ash conveying system, allowing the black water to fall into a stirring bin 4 for stirring treatment, controlling an outlet to a screw feeder 5 through a hydraulic gate valve, pressurizing the black water through a wet ash conveying pump 6, conveying the black water to a composite coal slime pipeline, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge 3 into a filtrate tank 9, and conveying the filtrate in the filtrate tank 9 back to the settling tank 1 through a pipeline by a filtrate pump 10.
Further, 15wt% of high solid content black water is sent to a centrifuge 3 for solid-liquid separation, the coal slime contains 35wt% of water, the coal slime is sent to a wet ash conveying system after being sent out of the centrifuge 3 and falls into a stirring bin 4 for stirring treatment, and the pasty coal slime with water content of 40% and pumpability contains water.
Further, a pipeline distributor 7 is further arranged between the wet ash conveying pump 6 and the boiler, and the pipeline distributor 7 is further connected with the intermediate slag yard.
Preferably, the boiler is fed with coal slurry at a location 800mm above the point of entry of the fuel coal.
Furthermore, a flushing water system is connected to the centrifuge 3, one path of the flushing water system is connected with the centrifuge 3, and the other path of the flushing water system is connected with the boiler through a flushing water pump 8.
Further, the sedimentation tank underflow pump 2 is also connected with a filter through a pipeline, and the sedimentation tank underflow pump 2 can be conveyed to the filter for filtering under the condition of maintenance of the centrifuge 3, the filter cake contains 45wt% of water, and the filter cake is directly loaded after being discharged from the filter.
Preferably, the centrifuge 3 is a horizontal screw centrifuge.
Example 2
The comprehensive recycling process of the gasified fine slag comprises the following steps: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank 1 to a centrifuge 3 through a settling tank underflow pump 2 for solid-liquid separation, discharging the black water out of the centrifuge 3 into a wet ash conveying system, allowing the black water to fall into a stirring bin 4 for stirring treatment, controlling an outlet to a screw feeder 5 through a hydraulic gate valve, pressurizing the black water through a wet ash conveying pump 6, conveying the black water to a composite coal slime pipeline, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge 3 into a filtrate tank 9, and conveying the filtrate in the filtrate tank 9 back to the settling tank 1 through a pipeline by a filtrate pump 10.
Further, 20wt% of high solid content black water is sent to a centrifuge 3 for solid-liquid separation, the coal slime contains 40wt% of water, the coal slime is sent out of the centrifuge 3 and then enters a wet ash conveying system, and the coal slime falls into a stirring bin 4 for stirring treatment, and the pasty coal slime with 50% of water content and pumpability contains water.
Further, a pipeline distributor 7 is further arranged between the wet ash conveying pump 6 and the boiler, and the pipeline distributor 7 is further connected with the intermediate slag yard.
Preferably, the boiler is fed with coal slurry at a location 800mm above the point of entry of the fuel coal.
Furthermore, a flushing water system is connected to the centrifuge 3, one path of the flushing water system is connected with the centrifuge 3, and the other path of the flushing water system is connected with the boiler through a flushing water pump 8.
Further, the sedimentation tank underflow pump 2 is connected with a filter through a pipeline, and the sedimentation tank underflow pump 2 can be sent to the filter for filtering under the condition of maintenance of the centrifuge 3, the filter cake contains 45-55 wt% of water, and the filter cake is directly loaded after being taken out of the filter.
Preferably, the centrifuge 3 is a horizontal screw centrifuge.
Example 3
The comprehensive recycling process of the gasified fine slag comprises the following steps: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank 1 to a centrifuge 3 through a settling tank underflow pump 2 for solid-liquid separation, discharging the black water out of the centrifuge 3 into a wet ash conveying system, allowing the black water to fall into a stirring bin 4 for stirring treatment, controlling an outlet to a screw feeder 5 through a hydraulic gate valve, pressurizing the black water through a wet ash conveying pump 6, conveying the black water to a composite coal slime pipeline, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge 3 into a filtrate tank 9, and conveying the filtrate in the filtrate tank 9 back to the settling tank 1 through a pipeline by a filtrate pump 10.
Further, 25wt% of high-solid-content black water is sent to a centrifuge 3 for solid-liquid separation, the coal slime contains 45wt% of water, the coal slime is sent out of the centrifuge 3 and then enters a wet ash conveying system, the wet ash conveying system falls into a stirring bin 4 for stirring treatment, and the pasty coal slime with 60% of water content and pumpability contains water.
Further, a pipeline distributor 7 is further arranged between the wet ash conveying pump 6 and the boiler, and the pipeline distributor 7 is further connected with the intermediate slag yard.
Preferably, the boiler is fed with coal slurry at a location 800mm above the point of entry of the fuel coal.
Furthermore, a flushing water system is connected to the centrifuge 3, one path of the flushing water system is connected with the centrifuge 3, and the other path of the flushing water system is connected with the boiler through a flushing water pump 8.
Further, the sedimentation tank underflow pump 2 is also connected with a filter through a pipeline, and the sedimentation tank underflow pump 2 can be sent to the filter for filtering under the condition of maintenance of the centrifuge 3, wherein the filter cake contains 55wt% of water, and the filter cake is directly loaded after being discharged from the filter.
Preferably, the centrifuge 3 is a horizontal screw centrifuge.
Aiming at the current situation of the problems existing in the comprehensive utilization of fine slag in the industry, Huayi company decides to adopt a technical route of a centrifuge and coal slime recycling to solve the problems through full investigation of related industries, and the technical advantages are mainly reflected as follows:
1) the centrifugal machine is a single-series device, auxiliary equipment is not needed in the coal slime dehydration process, the operation stability is high, the operation cost is low, and the operation cost is only 25% of that of the vacuum belt filtration system. Meanwhile, due to the principle of centrifugal dehydration, the water content of the dehydrated coal slime is maintained at 40-50%, and the dehydrated coal slime is rich in a large amount of surface water and completely has the condition of directly entering a coal slime recycling system.
2) The centrifugal machine is placed above the coal slime recycling bin, the whole process can realize the full-closed recycling of the coal slime, and the environment is friendly.
(2) Optimized stabilization of a centrifuge
The most critical condition for the stable operation of the centrifugal machine is that the concentration and the flow of the slime water at the input end must be stable. In order to match with the operating conditions of the centrifuge, a large amount of related systems are transformed according to the principle of starting from the requirement, so that the stable operation of the centrifuge is realized:
1) because the working conditions of each gasification furnace are inconsistent, the concentration and the speed of the settled coal slime of the settling tank are inconsistent, the settling tank underflow of the same frame is connected to an outward delivery pipeline for conveying by the design of the aerospace furnace, and the problem does not exist when the coal slime is conveyed to a belt filter because the treatment process of the belt filter can ensure the sufficient dehydration of the coal slime. The concentration is not uniform during the conveying process to the centrifugal machine. Hua Yi company researches and then separates pumping pipelines of bottom flow pumps of the settling tanks independently, and sends out the single settling tank, so that mutual interference caused by inconsistent outlet concentration of the bottom flow pumps is avoided, and the stability of the flow rate sent out by the bottom flow pumps of each settling tank is guaranteed.
2) After the flow temperature is reduced, the conveying concentration is not stable, and particularly when the load and the working condition of the space furnace are changed, the coal slime settling velocity deviation in the settling tank is large. Huayi company establishes a data analysis system by setting up the oil pressure of a settling tank raking machine, the frequency of an underflow pump and the solid content of coal slurry at the inlet of a centrifugal machine, summarizes the corresponding relation between the underflow pump and the oil pressure under each load and the solid content of the coal slurry at the outlet through data acquisition, analysis and comparison for nearly two months, establishes an operation data comparison table, determines the conveying frequency of the underflow pump under each working condition, and further stabilizes the concentration of the coal slurry at the inlet of the centrifugal machine.
3) The self failure rate of the centrifugal machine is higher at the beginning of operation. A washing water system of the centrifuge is added, and the centrifuge is stopped for washing periodically. And meanwhile, the oil seal system is optimized and improved. The operation stability of the centrifuge is greatly improved.
Through the adjustment, optimization and modification, the continuous stable operation of the centrifuge is realized from the initial stable operation time of not more than 1 hour to 24 hours.
(3) Demonstration optimization of coal slime recycling mode
The traditional coal slime recycling adopts the coal slime input from the top of a boiler. Through the research and full research on the brother manufacturers, the method for inputting the coal slime from the furnace top has a plurality of problems: firstly, the coal slime directly enters the top of the boiler to participate in the large circulation of the boiler, and because the granularity of the coal slime is very fine (average 90 microns), a large amount of the coal slime enters a subsequent cyclone separation system without participating in combustion, and the heat is not fully utilized. Meanwhile, because the top enters, a large amount of water brought by coal slime is evaporated at the upper part of the boiler, the outlet smoke temperature of the boiler is reduced, and certain influence is caused on subsequent high-temperature and low-temperature heat exchange. And the top feeding mode is adopted, and the coal slime is required to enter the boiler basically in a free landing mode, so that the pressure of the coal slime at the boiler inlet is very low, and the coal slime is difficult to enter the boiler when the boiler pressure fluctuates, particularly when negative pressure is not formed at the top of the boiler, and the coal slime is blocked. From the effect of actual operation, the mode of adopting top pan feeding does not reduce boiler coal consumption, and the ash carbon content obviously rises, and operating stability is relatively poor moreover, and the coal slime pipeline often blocks up, can not reach the expected effect of coal slime retrieval and utilization.
Fully demonstrated, because we adopt anthracite as fuel coal, the furnace temperature reaches 1000 ℃ when running, can completely adopt the mode of entering coal slime in the dense phase zone of the boiler, adopt the mode of dense phase zone feeding and will not cause serious influence to the furnace temperature, finally confirm that enters the coal slime at the position 800mm above the fuel coal point of entering the furnace, the technical characteristics of dense phase zone feeding are obvious:
because the circulating fluidized bed boiler using anthracite as raw material is adopted, the temperature of the hearth is generally controlled below 980 ℃ during operation, and when the load of the boiler is higher, the temperature of the hearth often exceeds 1000 ℃. And because the water content of the coal slime reaches 40-50 percent and the heat value is lower, a large amount of water can be instantly gasified after entering the hearth, and a certain cooling effect can be realized on a dense-phase region. Meanwhile, the coal slime enters a dense-phase area and can deflagrate instantly at a high-temperature section, residual carbon in the coal slime can be fully combusted, and the part of heat energy can be taken away by a large amount of smoke instantly.
Practice proves that after the dense-phase region coal slurry inlet mode is adopted, the functions are obvious:
1) the boiler steam fuel coal consumption is obviously reduced, the ton steam coal consumption of Huayi company is reduced from 118kg/t before coal slurry feeding to 108kg/t after coal slurry feeding, the residual carbon of boiler slag and furnace ash is not increased after coal slurry feeding, and the heat value of fine slag is also verified to be fully utilized.
2) The temperature of the hearth is effectively controlled, the temperature of the furnace operated before is about 1000 ℃, the temperature of the hearth is reduced to 920 ℃ plus 900 ℃ at present, low-nitrogen combustion is really realized, the content of nitrogen oxides is obviously reduced, and the ammonia water for denitration is reduced by nearly 80% after coal slime is used.
3) When the coal slime is not used, the load of the boiler is difficult to be increased to 240t/h which can only reach 220t/h due to the limitation of the temperature of a hearth, and the capacity of the boiler is not fully exerted. After the coal slime is used, the highest boiler load is increased to 254t/h due to the reduction of the furnace temperature, and the boiler capacity is fully released.
(4) Comparison of technical combinations
Now, the way of the project of Hua Yi company and the way of utilizing different fine slags adopted in the industry are comprehensively compared:
TABLE 1 Huayi company Fine slag recycle mode and industry internal ratio
Claims (7)
1. The comprehensive recycling process of the gasified fine slag is characterized by comprising the following steps of: the method comprises the steps of firstly, conveying high-solid-content black water from a settling tank to a centrifuge through a settling tank underflow pump for solid-liquid separation, conveying the black water out of the centrifuge into a wet ash conveying system, enabling the black water to fall into a stirring bin for stirring treatment, controlling an outlet to a screw feeder through a hydraulic gate valve, finally, conveying the black water to a composite coal slime pipeline after pressurization through a wet ash conveying pump, conveying the black water to a boiler for blending combustion utilization, automatically flowing filtrate of the centrifuge into a filtrate tank, and conveying the filtrate in the filtrate tank back to the settling tank through a pipeline through the filtrate pump.
2. The comprehensive recycling process of gasified fine slag according to claim 1, wherein the high solid content black water 15-25 wt% is sent to a centrifuge for solid-liquid separation, the coal slurry contains 35-45 wt% of water, the coal slurry is sent to a wet ash conveying system after being sent out of the centrifuge and falls into a stirring bin for stirring treatment, and the pasty coal slurry with water content of 40-60% and pumpability contains water.
3. The comprehensive recycling process of gasified fine slag according to claim 1, wherein a pipeline distributor is further arranged between the wet ash delivery pump and the boiler, and the pipeline distributor is further connected with an intermediate slag yard.
4. The process of claim 3, wherein the boiler is fed with coal slurry at a position 800mm above the point of feeding the fuel coal.
5. The comprehensive recycling process of the gasified fine slag according to any one of claims 1 to 2, wherein the centrifuge is further connected with a flushing water system, one path of the flushing water system is connected with the centrifuge, and the other path of the flushing water system is connected with a boiler through a flushing water pump.
6. The comprehensive recycling process of the gasified fine slag according to any one of claims 1 to 2, wherein the underflow pump of the settling tank is further connected with a filter through a pipeline, the underflow pump of the settling tank can be used for filtering through the filter under the condition of maintenance of a centrifuge, the filter cake contains 45-55 wt% of water, and the filter cake is directly loaded after being discharged from the filter.
7. The comprehensive recycling process of the gasified fine slag according to any one of claims 1 to 2, wherein the centrifuge is a horizontal screw centrifuge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202110966492.XA CN113562809A (en) | 2021-08-23 | 2021-08-23 | Comprehensive recycling process for gasified fine slag |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110966492.XA CN113562809A (en) | 2021-08-23 | 2021-08-23 | Comprehensive recycling process for gasified fine slag |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115490348A (en) * | 2022-09-16 | 2022-12-20 | 安徽海蓝生物科技有限公司 | Mother liquor recovery process and recovery equipment in L (+) -tartaric acid production process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115490348A (en) * | 2022-09-16 | 2022-12-20 | 安徽海蓝生物科技有限公司 | Mother liquor recovery process and recovery equipment in L (+) -tartaric acid production process |
| CN115490348B (en) * | 2022-09-16 | 2023-10-31 | 安徽海蓝生物科技有限公司 | Mother liquor recovery process and recovery equipment in L (+) -tartaric acid production process |
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Application publication date: 20211029 |