CN206281323U - A kind of system of utilization high-temperature semi-coke - Google Patents
A kind of system of utilization high-temperature semi-coke Download PDFInfo
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- CN206281323U CN206281323U CN201621325165.7U CN201621325165U CN206281323U CN 206281323 U CN206281323 U CN 206281323U CN 201621325165 U CN201621325165 U CN 201621325165U CN 206281323 U CN206281323 U CN 206281323U
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- 239000000571 coke Substances 0.000 title claims abstract description 40
- 239000003245 coal Substances 0.000 claims abstract description 193
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000000197 pyrolysis Methods 0.000 claims abstract description 28
- 239000000203 mixture Substances 0.000 claims abstract description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 239000003077 lignite Substances 0.000 abstract description 64
- 238000001035 drying Methods 0.000 abstract description 29
- 238000000034 method Methods 0.000 abstract description 15
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract 2
- 235000011941 Tilia x europaea Nutrition 0.000 abstract 2
- 239000004571 lime Substances 0.000 abstract 2
- 238000009833 condensation Methods 0.000 abstract 1
- 230000005494 condensation Effects 0.000 abstract 1
- 239000000843 powder Substances 0.000 description 13
- 238000000227 grinding Methods 0.000 description 10
- 238000002156 mixing Methods 0.000 description 7
- 238000007664 blowing Methods 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000011812 mixed powder Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002817 coal dust Substances 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000011363 dried mixture Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Coke Industry (AREA)
Abstract
The utility model discloses a kind of system of utilization high-temperature semi-coke.The system includes drying machine, elevator, pyrolysis oven, high-temperature semi-coke storehouse, lime set tank, water pump and heat exchanger；Wherein, the drying machine includes coal entrance, and the drying machine, the elevator, the pyrolysis oven and the high-temperature semi-coke storehouse order are connected；The drying machine also includes high-temperature steam entrance, water and Low Temperature Steam mixture outlet；The heat exchanger is arranged in the high-temperature semi-coke storehouse, and the heat exchanger includes high-temperature steam outlet, condenses water inlet；The high-temperature steam outlet is connected with the high-temperature steam entrance；The lime set tank and the water pump are disposed between the water and Low Temperature Steam mixture outlet and the condensation water inlet.The utility model takes full advantage of the exterior heat of high-temperature semi-coke, cancels cold burnt machine and simplifies technological process, produces steam to go drying raw coal (lignite) to reduce Boiler Steam using high warm semicoke and consumes.
Description
Technical Field
The utility model belongs to the technical field of coal pyrolysis and pulverized coal combustion electricity generation, especially, relate to a heat accumulation formula radiant tube heating granule coal is in order to prepare coal tar cogeneration system.
Background
China is rich in coal resources, and raw coal is mainly used for direct combustion except for partial coking and conversion processing. The coal is directly combusted, so that oil gas resources rich in the coal are not fully refined and utilized, the direct combustion heat efficiency is low, and the environment is seriously damaged. The pyrolysis of coal is to heat coal under inert atmosphere to prepare products such as semicoke, coal gas and tar, and the obtained products can be utilized in a gradient manner, so that the comprehensive utilization efficiency of coal, particularly lignite and long-flame coal, is improved while oil and gas resources are fully extracted, and the lignite is taken as an example for illustration.
The drying and pyrolysis of the lignite are important means for effectively utilizing the lignite, a large amount of steam is consumed for drying the lignite, meanwhile, the high-temperature semicoke after the lignite pyrolysis needs to be cooled to the normal temperature and then is conveyed to a medium-speed mill for grinding, a large amount of cooling water is consumed in the coke cooling process, and the related surface heat of the high-temperature semicoke cannot be fully utilized. In the grinding process of the mill, if raw coal is added, secondary heating and drying are needed, and partial heat is also needed to be consumed.
For example, the power plant semicoke milling and injection process disclosed in the prior art (see the attached figure 1) comprises the following process flows: raw coal from a lignite bin is dried by a dryer 2 and then lifted to a pyrolysis furnace 4 by a lifter 3, the lignite is pyrolyzed to become hot semicoke at the temperature of about 750 ℃, then the hot semicoke enters a coke cooler to be cooled to about 80 ℃, then the hot semicoke enters a semicoke bin 7 by the lifter 6, the raw coal enters a raw coal bin 9, the cold coke and the raw coal respectively enter an intermediate speed mill by a coke feeder 8 and a coal feeder 10 according to a certain proportion, the raw coal is further dried in the intermediate speed mill by high-temperature air 12 of a boiler heat exchanger, meanwhile, the raw coal and the semicoke are ground into powder, the powder is sent to a pulverized coal boiler 13 for combustion by drying air, most of steam generated by the boiler is sent to a steam turbine for power generation, and part of the steam returns to the dryer 2 for drying the raw coal. The prior art has the following disadvantages: (1) the steam generated by the boiler 13 is consumed for drying the raw coal (brown coal), so that the production efficiency of the system is reduced; (2) a large amount of cooling water is consumed by the coke cooler, so that the system cost is increased; (3) the surface heat of the high-temperature semicoke is not utilized; (4) high-temperature air is needed for drying raw coal in the medium-speed mill, and heat energy of a boiler heat exchanger needs to be consumed.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model discloses develop a new technology, the main problem of energy effective utilization around solving the lignite pyrolysis, utilize the high temperature table heat of pyrolysis back semicoke promptly, the dry heat source of raw coal before as the pyrolysis, also the dry heat source of raw coal in the coal pulverizer is as simultaneously to realize the table heat of make full use of high temperature semicoke, cancel the cold coke machine in order to simplify process flow, utilize the hot semicoke of high temperature to produce steam and go to dry raw coal (brown coal) in order to reduce the purpose of boiler steam consumption.
In order to realize the aim, the utility model provides a system utilizing high-temperature semicoke, which comprises a dryer, a hoister, a pyrolysis furnace, a high-temperature semicoke bin, a condensate tank, a water pump and a heat exchanger; wherein,
the dryer comprises a coal inlet, and the dryer, the hoister, the pyrolysis furnace and the high-temperature semi-coke bin are sequentially connected;
the dryer dries coal by using high-temperature steam to obtain a dried mixture of the coal, water and low-temperature steam; the hoister is used for conveying the dried coal to the pyrolysis furnace; the pyrolysis furnace is used for pyrolyzing coal from the elevator to obtain pyrolyzed high-temperature semicoke;
the dryer also comprises a high-temperature steam inlet and a mixture outlet of water and low-temperature steam; the heat exchanger is arranged in the high-temperature semi-coke bin and comprises a high-temperature steam outlet and a condensed water inlet; the high-temperature steam outlet is connected with the high-temperature steam inlet; the condensate tank and the water pump are sequentially arranged between the outlet of the mixture of the water and the low-temperature steam and the inlet of the condensate water;
the condensate tank is used for gas-liquid separation of the water and low-temperature steam mixture to obtain condensate water; the water pump is used for conveying the condensed water to the heat exchanger through a condensed water inlet; the heat exchanger is used for heat exchange between the pyrolyzed high-temperature semicoke and the condensed water to obtain the heat-exchanged high-temperature semicoke and the high-temperature steam.
Further, the system further comprises: coke feeder, raw coal bunker, coal feeder and coal pulverizer.
The coke feeder is arranged between the coal mill and the high-temperature semi-coke bin and is used for feeding the heat-exchanged high-temperature semi-coke into the coal mill.
The coal feeder is arranged between the coal mill and the raw coal bin and used for feeding raw coal into the coal mill.
And the coal mill is used for drying and grinding the high-temperature semicoke subjected to heat exchange and the raw coal to obtain coal powder and coke powder.
Furthermore, the system also comprises a coal bunker, the coal bunker comprises a coal outlet, the coal outlet is connected with the coal inlet, the coal bunker is also provided with a coal speed regulator, and the coal speed regulator is used for regulating the feeding speed of the coal.
Further, the system also comprises a pulverized coal boiler, the pulverized coal boiler comprises a pulverized coal inlet and a coke powder inlet, the coal mill also comprises a pulverized coal outlet and a coke powder outlet, the pulverized coal outlet and the coke powder outlet are connected with the pulverized coal inlet and the coke powder inlet, and the pulverized coal boiler is used for burning the pulverized coal and the coke powder.
Further, the coal mill further comprises an air inlet, normal-temperature air is introduced from the air inlet, the coal dust and the coke powder are fed into the coal dust boiler to be combusted, or high-temperature air is introduced from the air inlet to dry the raw coal.
Adopt the utility model discloses a system has gained following effect:
(1) the surface heat of the high-temperature semicoke is fully utilized, and the energy waste is reduced;
(2) the process is more simplified, and a coke cooling machine is omitted;
(3) the steam generated by the high-temperature semicoke is used for drying the lignite, so that the original consumption of the boiler steam is eliminated on the premise of ensuring safety, and the boiler efficiency is improved;
(4) the normal temperature air is used as coal supply air instead of high temperature air, so that the energy consumption is further reduced.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
FIG. 1 is a process flow chart of the semi-coke pulverizing and injecting process of the power plant of the utility model;
in FIG. 1, 1-brown coal bunker; 2-a dryer; 3, a hoisting machine; 4-a pyrolysis furnace; 5-a coke cooling machine; 6. a hoist; 7-a coke cooling bin; 8-a coke feeder; 9-raw coal bunker; 10-a coal feeder; 11-a coal mill; 12-high temperature air; 13-pulverized coal fired boiler;
FIG. 2 is a flow chart of a new process for making powder by comprehensively utilizing high-temperature semicoke according to the present invention;
in FIG. 2, 1-brown coal bunker; 2-a dryer; 3, a hoisting machine; 4-a steam pipeline; 5-a vapor condensate tank; 6, a water pump; 7-a heat exchanger; 8-a pyrolysis furnace; 9-high temperature semi-coke bin; 10-coke feeder; 11. a raw coal bunker; 12-a coal feeder; 13-normal temperature air; 14-a coal mill; 15-pulverized coal fired boiler.
Detailed Description
The following description of the embodiments of the present invention will be made in conjunction with the accompanying fig. 2 and examples to better understand the aspects of the present invention and its advantages in various aspects. However, the specific embodiments and examples described below are for illustrative purposes only and are not intended to limit the present invention.
The novel high-temperature semicoke grinding process comprises the following steps:
the drying machine indirectly dries the lignite through steam, the steam comes from a heat exchanger in a high-temperature semi-coke bin, water is changed into high-temperature steam through a heat exchanger 7 in a high-temperature semi-coke bin 9, and the high-temperature steam enters the drying machine through a pipeline 4 to dry raw coal;
after drying, condensing the water vapor into water and part of low-temperature steam, allowing the water vapor to enter a condensate tank 5 for further gas-liquid separation, allowing the condensed water to enter a heat exchanger 7 through a water pump 6 to be heated into water vapor, and allowing the water vapor to enter a dryer through a steam pipeline 4 to dry lignite;
steam generated by the heat exchanger enters the dryer 2 through the pipeline 4, after the steam indirectly exchanges heat in the dryer and the lignite, the lignite is heated and dried, meanwhile, most of the steam is condensed into water and enters the condensate tank, and then the water is heated into the steam through the heat exchanger in the semi-coke bin through the water pump;
after the high-temperature semicoke is cooled by the heat exchanger 7, the high-temperature semicoke and raw coal in the raw coal bin 11 respectively enter a coal mill 14 through a coke feeder 10 and a coal feeder 12 according to a certain proportion, and dried and ground coal powder and coke powder are fed into a boiler to be combusted through air to generate steam to drive a steam turbine to generate power.
In detail, the novel process of the utility model comprises the following steps:
(1) the lignite drying machine 2 coming out of the lignite bin 1 is dried and then enters the pyrolysis furnace 8 through the lifting machine 3. The dryer indirectly dries the lignite through steam.
(2) Steam comes from a heat exchanger in the high-temperature semi-coke bin, water is changed into high-temperature steam through the heat exchanger 7 in the high-temperature semi-coke bin 9, the high-temperature steam enters a drying machine through a pipeline 4 to dry lignite, and the water vapor is condensed into water and part of low-temperature steam after drying.
(3) The condensed water and part of the steam enter a condensate tank 5 for further gas-liquid separation, the condensed water enters a heat exchanger 7 through a water pump 6 to be heated into steam, and then the steam enters a dryer through a steam pipeline 4 to dry the lignite.
(4) The original temperature of the high-temperature semi-coke is about 650 plus 850 ℃, water is heated into steam through a heat exchanger in the high-temperature semi-coke bin 9, the temperature of the steam at an outlet is controlled by controlling the flow of the water pump 6, the temperature of the steam is controlled to be about 150 plus 250 ℃, and the condition of drying the lignite is met.
(5) Steam enters the dryer 2 through the pipeline 4, after the steam indirectly exchanges heat in the dryer and the lignite, the lignite is heated and dried, meanwhile, most of the steam is condensed into water and enters the condensate tank, and then the water is heated into the steam through the water pump in the heat exchanger in the semi-coke bin.
(6) The high-temperature semicoke is cooled by a heat exchanger 7 and then is reduced to 250-350 ℃, then the high-temperature semicoke and raw coal in a raw coal bin 11 enter a coal mill 14 through a coke feeder 10 and a coal feeder 12 according to a certain proportion, normal-temperature air 13 is introduced into the coal mill, the high-temperature semicoke is used as a heating agent to be mixed with the raw coal in the coal mill 14, then the raw coal is heated and dried, and dried and ground coal powder and coke powder are sent into a boiler to be combusted through the normal-temperature air, so that steam is generated to drive a steam turbine to generate electricity.
The invention will now be described with reference to specific examples, which are intended to be illustrative only and not to be limiting in any way.
Example 1
The embodiment provides a system for utilizing high-temperature semicoke, lignite enters a pyrolysis furnace after being dried to generate semicoke, semicoke and power coal enter a coal mill according to a certain proportion to be ground and dried, and the semicoke and the power coal are ground into pulverized coal and then enter a pulverized coal boiler to be combusted to generate steam to be sent to a steam turbine to generate power. Technical data of lignite are shown in table 1:
table 1: technical data of lignite:
the coal feeding amount of the lignite is designed to be 120t/h, the lignite enters a dryer through a feeder, the moisture Mt of the dried lignite is less than or equal to 10%, and then the lignite enters a pyrolysis furnace for pyrolysis.
After lignite is pyrolyzed, semicoke is produced, the yield is 65t/h, the outlet temperature of the semicoke is 750 ℃, and the semicoke parameters are as follows:
table 2: high temperature semicoke parameter
The heat capacity of the semicoke is 210J/(kg.K), the temperature is reduced from 750 ℃ to about 300 ℃ after the semicoke passes through the heat exchanger, the heat exchanger generates 0.6Mpa and 190 ℃ steam for 65-85 t/h, and the steam is sent to a drier for drying the lignite through a pipeline. The temperature of the water vapor is controlled by adjusting the flow rate of the water pump. Therefore, the water vapor required by lignite drying can be met by the steam generated by the heat exchanger without additional steam. The above steam completely replaces the steam introduced from the raw coal boiler.
The high-temperature semicoke and raw coal in the raw coal bin are mixed according to the weight ratio of 1:1, and the raw coal in the raw coal bin has the following parameters:
TABLE 3 raw coal data of raw coal bunker
The high-temperature semicoke reaches 300 ℃ after temperature adjustment, and enters the coal grinding through a coal feeder according to the proportion of 1:1Mixing and grinding, setting the respective feeding amount to be about 60t/h, totaling 120t/h, blowing coal feeding air into the grinding machine through a fan, and designing the air volume to be 250000Nm3And h, blowing the semicoke and the raw coal into a boiler through coal feeding air to burn and generate power after the semicoke and the raw coal are mixed and ground.
After entering a coal mill, the two materials are mixed with combustion-supporting air, the temperature after mixing is about 180 ℃, and the ground mixed powder enters a pulverized coal boiler to be combusted under the driving of the combustion-supporting air.
TABLE 4 Mill Outlet mix powder parameters
| Temperature of | Particle size (-200 mesh) | Volatile component Vad | Yield (t/h) | |
| 180℃ | ≥75％ | 10.5 | 120 | 250000 |
Example 2
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Technical data of lignite are shown in table 1:
table 1: technical data of lignite:
the coal feeding amount of the lignite is designed to be 100t/h, the lignite enters a dryer through a feeder, the moisture Mt of the dried lignite is less than or equal to 10%, and then the lignite enters a pyrolysis furnace for pyrolysis.
After lignite is pyrolyzed, semicoke is produced, the yield is 60t/h, the outlet temperature of the semicoke is 650 ℃, and the semicoke parameters are as follows:
table 2: high temperature semicoke parameter
The heat capacity of the semicoke is 210J/(kg.K), the temperature is reduced from 650 ℃ to about 250 ℃ after the semicoke passes through the heat exchanger, the heat exchanger generates 0.55Mpa and 65-85 t/h of 215 ℃ water vapor, and the water vapor is sent to a drier for drying the lignite through a pipeline. The temperature of the water vapor is controlled by adjusting the flow rate of the water pump. Therefore, the water vapor required by lignite drying can be met by the steam generated by the heat exchanger without additional steam. The above steam completely replaces the steam introduced from the raw coal boiler.
The high-temperature semicoke and raw coal in the raw coal bin are mixed according to the weight ratio of 1: the raw coal enters a coal mill according to the proportion of 0.5, and the raw coal parameters in the raw coal bin are as follows:
TABLE 3 raw coal data of raw coal bunker
The high-temperature semicoke is subjected to temperature regulation to reach 250 ℃, enters a coal mill for mixing and grinding with raw coal in a raw coal bunker according to the ratio of 1:0.5, and the feeding of the high-temperature semicoke is setThe amount is about 60t/h, the total amount is 90t/h, coal feeding air is blown into the mill by a fan, and the designed air volume is 250000Nm3And h, blowing the semicoke and the raw coal into a boiler through coal feeding air to burn and generate power after the semicoke and the raw coal are mixed and ground.
After entering a coal mill, the two materials are mixed with combustion-supporting air, the temperature after mixing is about 160 ℃, and the ground mixed powder enters a pulverized coal boiler to be combusted under the driving of the combustion-supporting air. The mill outlet mix powder parameters were as follows:
TABLE 4 Mill Outlet mix powder parameters
| Temperature of | Particle size (-200 mesh) | Volatile component Vad | Yield (t/h) | |
| 160℃ | ≥75％ | 10.0 | 90 | 250000 |
Example 3
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Technical data of lignite are shown in table 1:
table 1: technical data of lignite:
the coal feeding amount of the lignite is designed to be 120t/h, the lignite enters a dryer through a feeder, the moisture Mt of the dried lignite is less than or equal to 10%, and then the lignite enters a pyrolysis furnace for pyrolysis.
After lignite is pyrolyzed, semicoke is produced, the yield is 60t/h, the outlet temperature of the semicoke is 850 ℃, and the semicoke parameters are as follows:
table 2: high temperature semicoke parameter
The heat capacity of the semicoke is 210J/(kg.K), the temperature is reduced from 850 ℃ to about 350 ℃ after the semicoke passes through the heat exchanger, the heat exchanger generates 0.65Mpa and 250 ℃ steam for 65-85 t/h, and the steam is sent to a drier for drying the lignite through a pipeline. The temperature of the water vapor is controlled by adjusting the flow rate of the water pump. Therefore, the water vapor required by lignite drying can be met by the steam generated by the heat exchanger without additional steam. The above steam completely replaces the steam introduced from the raw coal boiler.
The high-temperature semicoke and raw coal in the raw coal bin are mixed according to the weight ratio of 1:2, the raw coal enters a coal mill, and the raw coal parameters in the raw coal bin are as follows:
TABLE 3 raw coal data of raw coal bunker
The temperature of the high-temperature semicoke reaches 350 ℃ after temperature adjustment, the high-temperature semicoke and raw coal in a raw coal bunker enter a coal mill for mixing and grinding through a coal feeder according to the proportion of 1:2, and the feeding amount of the high-temperature semicoke is set asAbout 60t/h, total 180t/h, and simultaneously blowing coal supply air into the mill by a fan, wherein the designed air volume is 250000Nm3And h, blowing the semicoke and the raw coal into a boiler through coal feeding air to burn and generate power after the semicoke and the raw coal are mixed and ground.
After entering a coal mill, the two materials are mixed with combustion-supporting air, the temperature after mixing is about 200 ℃, and the ground mixed powder enters a pulverized coal boiler to be combusted under the driving of the combustion-supporting air. The mill outlet mix powder parameters were as follows:
TABLE 4 Mill Outlet mix powder parameters
| Temperature of | Particle size (-200 mesh) | Volatile component Vad | Yield (t/h) | |
| 200℃ | ≥75％ | 10.5 | 180 | 250000 |
Example 4
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Technical data of lignite are shown in table 1:
table 1: technical data of lignite:
the coal feeding amount of the lignite is designed to be 110t/h, the lignite enters a dryer through a feeder, the moisture Mt of the dried lignite is less than or equal to 10%, and then the lignite enters a pyrolysis furnace for pyrolysis.
After lignite is pyrolyzed, semicoke is produced, the yield is 65t/h, the outlet temperature of the semicoke is 750 ℃, and the semicoke parameters are as follows:
table 2: high temperature semicoke parameter
The heat capacity of the semicoke is 210J/(kg.K), the temperature is reduced from 750 ℃ to about 300 ℃ after the semicoke passes through the heat exchanger, the heat exchanger generates 0.55Mpa and 150 ℃ steam for 65-85 t/h, and the steam is sent to a drier for drying the lignite through a pipeline. The temperature of the water vapor is controlled by adjusting the flow rate of the water pump. Therefore, the water vapor required by lignite drying can be met by the steam generated by the heat exchanger without additional steam. The above steam completely replaces the steam introduced from the raw coal boiler.
The high-temperature semicoke and raw coal in the raw coal bin are mixed according to the weight ratio of 1:1.2, the raw coal enters a coal mill, and the parameters of the raw coal in a raw coal bin are as follows:
TABLE 3 raw coal data of raw coal bunker
The high-temperature semicoke is subjected to temperature regulation to reach 300 ℃, and enters a coal mill for mixing and grinding with raw coal in a raw coal bunker according to the ratio of 1:1.2, the feeding amount of the high-temperature semicoke is set to be about 60t/h, the total is 132t/h, meanwhile, coal feeding air is blown into the mill through a fan, and the designed air volume is 250000Nm3And h, blowing the semicoke and the raw coal into a boiler through coal feeding air to burn and generate power after the semicoke and the raw coal are mixed and ground.
After entering a coal mill, the two materials are mixed with combustion-supporting air, the temperature after mixing is about 180 ℃, and the ground mixed powder enters a pulverized coal boiler to be combusted under the driving of the combustion-supporting air. The mill outlet mix powder parameters were as follows:
TABLE 4 Mill Outlet mix powder parameters
| Temperature of | Particle size (-200 mesh) | Volatile component Vad | Yield (t/h) | |
| 180℃ | ≥75％ | 10.2 | 132 | 250000 |
Claims (5)
1. A system for utilizing high-temperature semicoke comprises a dryer, a lifter, a pyrolysis furnace, a high-temperature semicoke bin, a condensate tank, a water pump and a heat exchanger; wherein,
the dryer comprises a coal inlet, and the dryer, the hoister, the pyrolysis furnace and the high-temperature semi-coke bin are sequentially connected;
the dryer also comprises a high-temperature steam inlet and a mixture outlet of water and low-temperature steam; the heat exchanger is arranged in the high-temperature semi-coke bin and comprises a high-temperature steam outlet and a condensed water inlet; the high-temperature steam outlet is connected with the high-temperature steam inlet; the condensate tank and the water pump are sequentially arranged between the outlet of the mixture of the water and the low-temperature steam and the inlet of the condensate.
2. The system of claim 1, further comprising: a coke feeder, a raw coal bunker, a coal feeder and a coal mill; wherein,
the coke feeder is arranged between the coal mill and the high-temperature semi-coke bin;
the coal feeder is arranged between the coal mill and the raw coal bin.
3. The system of claim 2,
the system further comprises a coal bunker, the coal bunker comprises a coal outlet, the coal outlet is connected with the coal inlet, and the coal bunker is further provided with a coal speed regulator.
4. The system of claim 2,
the system further comprises a pulverized coal boiler, the pulverized coal boiler comprises pulverized coal and coke powder inlets, the coal pulverizer further comprises pulverized coal and coke powder outlets, and the pulverized coal and coke powder outlets are connected with the pulverized coal and coke powder inlets.
5. The system of claim 2, wherein the coal mill further comprises an air inlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621325165.7U CN206281323U (en) | 2016-12-05 | 2016-12-05 | A kind of system of utilization high-temperature semi-coke |
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| CN201621325165.7U CN206281323U (en) | 2016-12-05 | 2016-12-05 | A kind of system of utilization high-temperature semi-coke |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107965747A (en) * | 2017-12-12 | 2018-04-27 | 北京神雾电力科技有限公司 | A kind of pre- heat utilization system of semicoke and technique |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107965747A (en) * | 2017-12-12 | 2018-04-27 | 北京神雾电力科技有限公司 | A kind of pre- heat utilization system of semicoke and technique |
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